AppendiksA
APPENDIKSA PERIDTUNGAN NERACA MASSA
Kapasitas
Basis fasa
: 15.000 tonltahun
: NH3 gas
Udara gas
Suhu refrensi : 25°C
1. OKSIDATOR 1 (R-21O)
NH3 -..j OksidatoT 1 ~ O2, NO, N2, H20
Udara
Dari Ullman vol.A.17
Reaksi: NH3 (g) + ! 02 (g) _~~ NO (g) + ~ H20 (g) (96%)
313 NH3 (g) + 402 (g) • 2"N2 (g) + 2" H2O (g) (4%)
NH3 masuk dengan kadar 99,5 % = 428,9937 kg/jam
NH3 = 0,995 x 428,9937 = 426,8487 kg/jam
H2O = 0,005 x 428,9937 = 2,1450 kg/jam
Udara masuk: dianggap 60% jenuh
humidity = 0,0175 kg H20/kg udara kering
Udara masuk: = 7681,9666 kg/jam
H20= 0,0175 x76819666=1321223knl"am 0,0175 + l ' , 5'J
N2 = 079 x 7681,9666- 132,1223 x 28 = 5790 6573 knl"am , 2884 ' 5') ,
02 = 0,21 x 7681,9666-132,1223 x 32 = 17591870 knl"am 2884 ' 5') ,
Reaksi (1)
NH3 mula-mula = 25,1087 kmol/jam
Prarencana Pabrik Asam Nitrat
A-I
NH3 yang bereaksi = 0,96 x 25,1087 = 24,1044 lanol/jam
NH3 sisa = 25,1087 - 24,1044 = 1,0043 lanol/jam
02 mula-mula = 54,9746 lanol/jam
02 bereaksi = ~ x 24,1044 = 30,1305 kmol/jam 4
02 sisa = 54,9746 - 30,1305 = 24,8441 lanol/jam
NO hasil = 24,1044 lanol/jam
H2O hasil = ~x 24,1044 = 36,1566 lanol/jam 2
Reaksi (2)
NH3 bereaksi = 1,0043 lanoI/jam
02 bereaksi = ~x 1,0043 = 0,7533 kmol/jam 4
02 sisa = 24,8441 - 0,7533 = 24,0908 lanol/jam
N2 hasil = !x 1,0043 = 0,5022 lanol/jam 2
H2O hasil = ~x 1,0043 = 1,5065 lanol/jam 2
Neraca massa pada oksidator 1 :
Masuk, kg/jam Keluar, kg/jam
02 1759,1870 02 770,9067
N2 5790,6573 N2 5804,7182
H2O 134,2672 H2O 812,2035
NH3 426,8487 NO 723,1320
Total = 8110,9603 Total = 8110,9603
Prarencana Pabrik Asam Nitrat
A-2
AppendiksA
2. OKSIDATOR 2 (R-230)
O2, NO, N2, H20 --.,- Oksidator 2 1---. 02, H20, N2, NO, N02
Reaksi: NO (g) + !02 (g)---+. N02 (g) 2
Dari recycle diperoleh :
02 = 324,8375 kg/jam
N2 = 5804,7182 kg/jam
NO = 158,3967 kg/jam
N02 = 32,8833 kg/jam
Gas masuk oksidator 2 :
(95%)
02 = 770,9067 + 324,8375 = 1095,7442 kg/jam = 34,2420 kmol/jam
N2 = 5804,7182+ 5804,7182 = 11609,4364 kg/jam
H2O = 812,2035 kg/jam
NO = 158,3967 + 723,1320 = 881,5287 kg/jam = 29,3843 kmol/jam
N02 = 32,8833 kg/jam
NO yang bereaksi = 0,95 x 29,3843 = 27,9151 kmol/jam
NO sisa = 29,3843 - 27,9151 = 1,4692 kmol/jam = 44,0764 kg/jam
02 bereaksi = ! x 27,9151 = 13,9575 kmol/jam 2
02 sisa = 34,2420 - 13,9575 = 20,2845 kmol/jam = 649,1030 kg/jam
N02 hasil = 27,9151 kmol/jam = 1316,9767 kg/jam
Neraca massa pada oksidator 2 :
Masuk, kg/jam Keluar, kg/jam
02 1095,7442 02 649,1030
N2 11609,4364 N2 11609,4364
H2O 812,2035 H2O 812,2035
NO 881,5287 NO 44,0764
N02 32,8833 N02 1316,9767
Total = 14431,7960 Total = 14431,7960
Prarencana Pabrik Asam Nitrat
A-3
AppendiksA
3. KONDENSOR (E-212)
02, N2, H20,
NO, N02
--+I kondensor ~O, N02, N2, 02, H20
l H2O liq
Suhu keluar kondensor = 35°C
Jumlah gas-gas masuk = 14431,7980 kg/jam
Tekanan uap air pada suhu 35°C = 42,1750 mmHg = 0,055 attn
x p --=-G -x P'olal
x 0,055 =--
14431,7980-x 9,37
H2O yang terikut dalam gas keluar kondensor (x) = 84,9785 kg/jam
H2O yang mengembun = 812,2035 - 84,9785 = 727,2250 kg/jam
Neraca massa pada kondensor :
Masuk, kg/jam Keluar, kg/jam
Bagian atas :
02 1095,7442 02 649,1030
N2 11609,4364 N2 11609,4364
H2O 812,2035 H2O 84,9785
NO 881,5287 NO 44,0764
N02 32,8833 N02 1316,9767
Bagian bawah :
H20liq 727,2250
Total = 14431,7960 Total = 14431,7960
. Prarencana Pabrik Asaro Nitrat
A-4
.,
AppendiksA
, 4. ABSORBER (D-240)
02,N2 NO, N02
NO, N02 N2,02, H20
H20
HN03, H20
Reaksi : 3 N02 (g) + H20(!) --. 2 HN03 (I) + NO (g)
N02 masuk = 1316,9767 kg/jam = 28,6299 kmol/jam
N02 bereaksi = 0,95 x 28,6299 = 27,1984 kmol/jam
N02 sisa = 28.6299 - 27,1984 = 1,4315 kmol/jam
H2O bereaksi = .!..x 27,1984 = 9,0661 kmol/jam 3
HN03 hasil = ~x 27,1984 = 18,1323 kmoUjam 3
(95%)
NO keluar absorber = 9,0661 + 1,4692 = 10,5354 kmoUjam = 316,0608 kg/jam "
Untuk menghasilkan HN03 60% maka H2O yang ditambahkan
= 839,7682 kg/jam
Neraca massa pada absorber:
Masuk, kg/jam Keluar, kg/jam
Bagian atas: Bagian atas :
H2O 839,7682 02 649,1030
Bagian bawah: N2 11609,4364
N2 11609,4364 NO 316,0608
NO 44,0764 N02 65,8488
N02 1316,9767 Bagian bawah:
02 649,1030 HN03 1142,3342
H2O 84,9785 H2O 727,2250
Total = 14544,3392 Total = 14544,3392
Prarencana Pabrik Asam Nitrat
A-5
AppendiksB
APPENDIKSB
PERHITUNGAN NERACA PANAS
Burner ( Q - 211 )
Udara dari kompresor 306,25°C
Amonia dari tanki 30°C
i Flue gas
Burner
Udara LNG
Campuran gas ke oksidator 1 900°C
Bahan bakar yang digunakan LNG dengan komposisi :
metana = 87,1 %
etana = 3,41 %
propana = 1,73 %
N2 =7,1 %
CO2 =0,31 %
Helium = 0,35 %
Dari Perry ed. 7 :
Heating value = 86000 Btu / gal
Panas bahan masuk :
Tekanan pada burner = 9,86 atm
Suhu amonia masuk = 30°C
T = 30 + 25 = 2750C = 8150F 2 ' ,
B-1
AppendiksB
Massa NH3 masuk: = 426,8487 kg I jam = 25,1087 kmol/jam
Massa H20 masuk = 2,1450 kg I jam = 0,1192 kmol/jam
Dari Kern fig. 3 :
Cp NH3 = 0,52 Btu lib OF = 0,52 kkal I kg °C
Cp H20 = 0,44 Btu lib of = 0,44 kkal I kg °C
Hig NH3 = m * Cp * ~T = 426,8487 * 0,52 * (30 - 25) = 1109,8066 kkal
Hig H2O = m * Cp * ~T = 22,2553 * 0,44 * ( 30 - 25 ) = 48,9617 kkal
Dari Smith Van Ness app.B
Tc NH3 = 405,7 K
Pc NH3 = 112,8 atm
(j) NH3 = 0,253
Tr NH3 30 + 273 0,7469 405,7
Pr NH3 = 9.86 = 0 0874 112,8 '
Dari Smith Van Ness app B:
Tc H2O = 647,1 K
Pc H2O = 220,5 atm
(j) H2O = 0,345
Tr H2O = 30 + 273 0,4682 647,1
Pr H2O = 9,86 = 0 0447 220,5 '
B-2
AppendiksB
(HR~H3 = « -0,1607 + 0,253. (-0,2704) ). 8,314 . 405,7) / 4,2
= -183,9976 kkallkmol
= -183,9976 kkallkmol x 25,1087 kmol = - 4619,9485 kkal
(HR)H2o=« -5,5581 + 0,345. (-8,6339».8,314.647,1)/4,2
= -10935,2070 kkallkmol
= -10935,2070 kkallkmol x 0,1192 kmol = -1303,0930 kkal
HNH3 = HigNH3 + (HR~3 = 1109,8067 + -4619,9485 = -3510,1418 kkal
HH20 = HisH20 + (HR)H2o = 4,7189 + -1303,0903 = -1298,3741 kkal
Udara masuk pada suhu = 306,25°C
Suhu rata-rata = (306,25 + 25 )/2= 18~,62°C
Massa N2 masuk = 5790,6573 kg / jam = 206,8092 kmoVjam
Massa 02 masuk = 1759,1870 kg/jam = 54,9746 kmoVjam
Massa H20 masuk = 132,1223 kg / jam = 7,3401 kmoVjam
Dari Kern fig. 3 :
Cp N2 = 0,26 Btu / lb of = 0,26 kkal / kg °C
Cp 02 = 0,23 Btu / lb of = 0,23 kkal / kg °C
Cp H20 = 0,46 Btu / lb OF = 0,46 kkal / kg °C
HiS N2 = m * Cp * ilT = 5790,6573 * 0,26 * (306,25 - 25 )= 423435,6523 kkal
His 02 = m * Cp * ilT = 1759,1870 * 0,23 * (306,25 - 25 )= 113795,7547 kkal
His H2O = m * Cp * ilT = 132,1223 * 0,46 * (306,25 - 25)= 17093,0706 kkal
Dari Smith Van Ness app.B
.Ie N2 = 126,2 K Te H2O = 647,1 K
PeN2 =34 atm Pc H2O = 220,5 atm
B-3
Appendiks B
ro NH2 = 0,0,038
Tc 02 = 154,6 K
Pc 02 = 50,43 atm
ro 02 = 0,022
Tr N2 306,25 + 273 4,5899 126,2
PrN2 = 9.86 = ° 29 34 '
Tr 02 306,25 + 273 3,7467 154,6
Pr 02 = 9.86 = ° 1955 50,43 '
Dati Smith Van Ness app B:
(HR)o -'-R-T~02 = - 0,0018
c
ro H2O = 0,345
Tr H2O = 306,25 + 273 0,8951 647,1
Pr H2O = 9,86 = 0 0447 220,5 '
(HRi -"-----'-- H2O = -0 0641
RT ' c
R . . (H ~2 = (( -0,0023 + 0,038. 0,0237 ). 8,314 . 126,2) / 4,2
= -0,3496 kkaJJkmo1
Prarencana Pabrik Asam Nitrat
B-4
AppendiksB
= -0,3496 kkallkmol x 206,6092 kmol = -72,2989 kkaI
(HR)02 = « -0,0118 + 0,022. 0,0308 ). 8,314. 154,6) / 4,2
= -3,4038 kkallkmol
= -3,4038 kkallkmol x 54,9746 kmol = -187,1245 kkal
(HR)mo = « -0,0533 + 0,345. (-0,0641)).8,314.647,1) 14,2
= -96,6022 kkallkmol
= -96,6022 kkal/kmol x 7,3401 kmol = -709,0723 kkal
HN2 = HigN2 + (HR)N2 = 423435,6523 + -72,2989 = 423363,3534 kkal
Ho2 = Hig02 + (HR)02 = 113795,7547 + -187,1245 = 113608,6301 kkal
Hmo = HigH20 + (HR)H2o = 17093,0706 + -96,6022 = 16383,9983 kkal
Panas bahan masuk:
HN2 = 423363,3534 kkal
Ho2 = 113608,6301 kkal
HH20 = 16383,9983 kkal
HNH3 = -3510,1418 kkal
Hmo = -1298,3741 kkal
548547,4660 kkal
Panas bahan keluar :
Suhu gas keluar = 900°C
T = 900 + 25 = 864 5 OF 2 '
Dari Kern fig. 3 :
Cp NH3 = 0,59 Btu lIb OF = 0,59 kkall kg °C
B-5
Al1l1endiks 8
Cp H20 = 0,47 Btu / Ib OF = 0,47 kkaI / kg °C
Cp N2 = 0,26 Btu / Ib of = 0,26 kkaI / kg °C
Cp O2 = 0,235 Btu / Ib of = 0,235 kkal / kg °C
HigNH3 = m ... Cp ... i1T = 426,8487'" 0,59 ... (900 - 25) = 220360,6576 kkaI
HigH20 = m ... Cp'" i1T = 134,2672 ... 0,47'" (900 - 25) = 55217,4042 kkal
HigN2 = m ... Cp'" i1T = 5790,6573'" 0,26'" (900 - 25) = 1317374,5351 kkaI
Hig02 = m'" Cp'" i1T = 1759,1870'" 0,235'" (900 - 25) = 361732,8324 kkal
Dari Smith Van Ness app.B
Tc N2 = 126,2 K
PcN2=34atm
0) N2 = 0,0,038
Tc 02 = 154,6 K
Pc 02 = 50,43 atm
0) 02 =0,022
Tr N2 900 + 273 - 9 2948 126,2 '
PrN2 = 9.86 = 0 29 34 '
Tr 02 900 + 273 7,5873 154,6
Pr 02 = 9.86 = 0 1955 50,43 '
Prarencana Pabrik Asam Nitrat
Tc H20 = 647,1 K
Pc H2O = 220,5 atm
0) H2O = 0,345
Tc NH3 = 405,7 K
Pc NH3 = 112,8 atm
0) NH3 = 0,253
Tr H2O = 900 + 273 1,8127 647,1
Pr H2O = 9,86 = 0 0447 220,5 '
Tr NH3 = 900 + 273 2,8913 154,6
PrNH3= 9.86=0195 50,43 '
8-6
AppendiksB
Dari Smith Van Ness app B:
(HR)I =00419 RT N2 ,
c
(HR)' = 00011 RT H2O ,
c
(HR)I = 0 0385 RT 02 ,
c
(HR)I ~~. '-- = 0 0 I 22
RT NH3 , c
(HR~2 = « 0,0039 + (0,038.0,0419) ). 8,314. 126,2) / 4,2
= 1,3720 kkallkmol
= 1,3720 kkallkmol x 206,6092 kmol = 7945,0071 kkal
(HR)02 = « -0,0007 + (0,022. 0,0385) ). 8,314 . 154,6) / 4,2
= 0,045 kkallkmol
= 0,045 kkallkmol x 54,9746 kmol = 2,4731 kkal
(HR)H20 = « -0,0149 + (0,345.0,0011».8,314.647,1) / 4,2
= -18,60 kkallkmol
= -18,60 kkallkmol x 7,3401 kmol = -138,7431 kkal
(HR)mu = « -0,0066 + (0,253. 0,0122) ). 8,314. 647,1) / 4,2
= -4,4278 kkallkmol
= -4,4278 kkallkmol x 25,1087 kmol = -111,1758 kkal
HN2 = HigN2 + (HR~2 = 1317374,5351 + 7945,0071 = 1325319,5423 kkal
Prarencana Pabrik Asam Nitrat
B-7
AppendiksB
H02 = Hig02 + (HR)02 = 361732,8324 + 2,4731
Hmo = HigmO + (HR)mo = 55217,4042 + -138,7431
361735,3056 kkal
55078,6611 kkal
HNH3 = HigNH3 + (HR~3 = 220360,6576 + -111,1758 = 220249,4818 kkal
1962382,9908 kkal
Panas yang dibutuhkan = panas keluar - panas masuk
= 1962382,9908 - 548547,4660
= 1413835,5248 kkal / jam
Reaksi yang terjadi: CRt + 202 --. CO2 + 2H20 (I)
7 C2~ + - O2 --. 2C02 + 3H20 (2)
2
Kebutuhan O2 :
Reaksi 1 :
O2 yang bereaksi = 2 * 0,0544 x kmol
C02 hasil = 0,0544 x kmol
H20 hasil = 0,1088 x kmol
Reaksi 2:
O2 yang beraksi = ~ * 1,1367.10-3 = 3,9785.10-3 x kmol
CO2 hasil = 2 * 1,1367.10-3 X = 2,2734.1O-3x kmol
H20 hasil = 3 * 1,1367.10-3 X = 3,4101.1O-3x kmol
Reaksi 3 :
02 yang bereaksi = 5 * 3,9318.104 X = 1,9659.1O-3x kmol
C02 hasil = 3 * 3,9318.104 X = 1,1795.1O-3xkmol
B-8
Appendiks B
H20 hasil = 4 * 3,9318.10-4x = 1,3567. 10-3 X kmol
Kebutuhan O2 = 0,1088 + 3,9785.10-3 + 1,9659.10-3 = 0,1147 x kmol
O2 yang ditambahkan 15 % berlebih = 1,15 * 0,1147 x = 0,1319 x kmol
= 4,2226 x kg / jam
N2 yang masuk = 79 * 4,2226x = 0,4392x kmol = 13,8935 x kg / jam 21
O2 sisa = 0,1319 x - 0,1147 x = 0,0172 x kmo!
C02 hasil = 0,0544 x + 2,2734.1O-3x + 1,1795.1O-2x + 7,0455.1O-5x
= 0,0685 x kmol
H20 hasil = 0,1088 + 3,4101.1O-3x + 1,3567.1O-3x = 0,1136 x kmo!
Kebutuhan bahan bakar :
Basis kebutuhan bahan bakar = x kg
C~ = 87,1 % = 0,87lx kg = 0,0544 x kmo!
C2~= 3,41 % = 0,341x kg = 1,1367.10-3 x kmo!
C3~= 1,73 % = 0,00173x kg= 3,9318.10-4 xkmol
N2 = 7,1 % = 0,0071x kg = 2,5357.10-3 x kmo!
C02 = 0,31 % = 0,0031x kg = 7,0455.10-5 x kmol
He = 0,35 % = 0,0035x kg = 8,75.10-4 x kmol
Panas yang dihasilkan :
1. Bahan bakar
Suhu bahan bakar masuk = 30°C = 303 oK
T = 303 + 298 = 300 5 OK 2 '
"T" ~ .'
B-9
AppendiksB B-I0
Dari Kern, fig,5 :
Cp CH4 = 0,852 kkal / kg °C
Cp C2~ = 0,65 kkal / kg °C
Cp C3~ = 0,45 kkal / kg °C
Cp N2 = 0,255 kkal / kg °C
Cp CO2 = 0,21 kkal/ kg °C
Dari Perry, ed,7, tab.2-194
Cp He = 4,97 kkal/ kmol °C
H CH4 = m * Cp * ~T = 0,871x * 0,852 * (900-25) = 3,7105 x kkal
H C2H6 = m * Cp * ~T = 0,0341 x * 0,65 * (900-25) = 0,1108 x kkal
H C3H6 = m * Cp * ~T = 0,0173 x * 0,45 * (900-25) = 0,0389 x kkal
H N2 = m * Cp * ~T = 0,071 x * 0,255 * (900-25 ) = 0,0905 x kkal
H C02 = m * Cp * ~T = 0,0031 x * 0,21 * (900-25) = 0,0032 x kkal
H He = m * Cp * ~T = 8,75,10-4 x * 4,97 * (900-25 ) = 0,0217 x kkal
Panas bahan bakar total = 2,7962 x kkal
2, Panas udara
Suhu udara masuk = 30°C = 303 OK
T = 303 + 298 300 5 OK 2 '
Dari Perry ed, 6 tab, 3 -181 :
Cp 02 = 6,269 kkal / kmol OK
Cp N2 = 6,801 kkall kInol OK
Prarencana Pabrik Asam Nltrat
AppendiksB
H 02 = m * Cp * ..1T = 0,1319 x * 6,269 * (303-298) = 4,1344 x kkal
H N2 = m * Cp * ..1T = 0,4962 x * 6,801 * ( 303-298 ) = 16,8733 x kkal
3. Panas Pembakaran
Heating value = 86000 Btu / gal
p = 3,4469 lb/gal
Hv = 86000 24949,45 btu/1b = 13869,9122 kkal/kg 3,4469
H = m * Hv = x * 13869,9122 = 13869,9122 x kkal
Menghitung panas flue gas keluar :
CO2 = 0,0685 x kmol = 3,014 x kg
H20 = 0,1136 x kmol = 2,0448 x kg
He = 8,75.104 x kmol
02 = 0,0172 x kmol
= 21,0077 x kkal
N2 = 0,4962 x + 2,535.10-5 x = 0,4962 x kmol = 13,8936 x kmol
Suhu flue gas keluar = 1200 °C = 1473 oK
T= 1473+298 =8855 oK 2 '
Dari Kern, fig.3 :
Cp CO2 = 0,29 kkal / kg °C
Cp H20 = 0,5 kkal / kg °C
Cp O2 = 0,25 kkal / kg °C
Cp N2 = 0,265 kkal / kg °C
B-ll
DA~QQ~eillnd~ik~s£B __________________________________________ ~~B~-12
Dari Perry, ed.7. tab.2-194 :
Cp He = 4,97 kkal / kmol °C
H CO2 = m * Cp * ilT = 3,014 x * 0,29 * ( 1200-25 )
H H2O = m * Cp * ilT = 2,0448 x * 0,5 * ( 1200-25 )
H 02 = m * Cp * ilT = 0,5504 x * 0.25 * ( 1200-25 )
1027,0205 x kkal
1201,3200 x kkal
161,6800 x kkal
H N2 = m * Cp * il T = 13,8936 x * 0,265 * ( 1200-25 ) = 4326,1190 x kkal
H He = m * Cp * ilT = 8,75.10-4 x * 4,97 * ( 1200-25) = 5,1098 x kkal
= 6721,2493 x kkal
Panas yang hilang = 20 % dari panas pembakaran
= 0,2 * 13869,9122 x
= 2773,9824 x kkal
Panas masuk :
Panas bahan = 548547,4660 kkal
Panas bahan bakar = 3,9756 x kkal
Panas pembakaran = 13869,9122 x kkal
Panas udara _=-=2",-1.~0:!!...07,-,7,--,x~kk~a~1 _____ _
= ( 548547,4660 + 13894,8955 x) kkaI
Panas keluar :
Panas bahan
Panas flue gas
= 1962382,9908 kkal
= 6721,2493 x kkal
Panas yang hilang = 2773,9824 x kkal
= ( 1962382,9908 + 9495,2317 x ) kkal
Prarencana Pabrik Asam Nitrat
AppendiksB
Panas masuk = panas keluar
548547,4660 + 13894,8955 x = 1962382,9908 + 9495,2317 x
x = 321,3508 kg / jam
Panas bahan bakar = 3,9756 x = 3,9756 * 321,3508 = 1277,5623 kkal
Panas pembakaran = 13869,9122 x = 13869,9122 * 321,3508
Panas udara
Panas flue gas
= 4457107,381 kkal
= 21;0077 x = 21,0077 * 321,3508 = 6750,8412 kkal
= 6721,2493 x = 6721,2493 * 321,3508
= 2159878,84 kkal
Panas yang hilang = 2773,9824 x = 2773,9824 * 321,3508
= 891421,4634 kkal
Neraca panas :
Masuk Kkal/jam Keluar kkal / jam
Panas bahan 548547,4660 Panas bahan 1962382,9908
Panas udara 6750,8412 Panas flue gas 2159878,8400
Panas pembakaran 4457107,3810 Panas yang hilang 891421,4634
Panas bahan bakar 1277,5623
Total 5013683,2510 5013683,2510
Prarencana Pahrik Asam NitTat
B-13
~Ampp~elliooillikgs~B~ _____________________________________________ B~-14
2. Oksidator 1 ( R - 210 )
. burner Campuran gas dan 900°C ~ ...
steam 200 °C
Oksidator 1
, kondensat 200°C
~
•
Campuran gas ke HE 900°C
5 Reaksi: NH3 + - 02
4
3 __ .~ NO + - H20 Mil = -54,3062 kkal / mol
2
3 NH3 + - O2
2 1 3
--•• - N2 + - H20 ~H2 = -75,8373 kkal / mol 2 2
NH3 yang bereaksi pada reaksi 1 = 24,1044 kmol = 24104,4 mol
.lli,.l = 24104,4· (-54,3062) = -1309018,311 kkall jam
NH3 yang bereaksi pada reaksi 2 = 1,0043 kmol = 1004,3 mol
MIrl = 1004,3 • ( -75,8373) = -76167,1890 kkal / jam
Panas reaksi eksotermis = MIrl + ~Hr2
Panas masuk :
Suhu gas masuk = 900°C
= -1309018,311 + (-76167,1890)
= -1385185,5000 kkal / jam
T = 900 + 25 = 462 5 °C = 864 5 OF 2 ' ,
Dari Kern fig. 3 :
Cp NH3 = 0,66 Btu / Ib OF = 0,66 kkal / kg °C
Prarencana Pabrik Asaro Nitrat
AppendiksB
Cp H20 = 0,49 Btu / Ib of = 0,49 kkal / kg °C
Cp N2 = 0,26 Btu / Ib OF = 0,25 kkai/ kg °C
Cp O2 = 0,245 Btu / Ib OF = 0,265 kkal / kg °C
HigNH3 = m * Cp * L\T = 426,8487 * 0,66 * ( 900 - 25) = 246505,1424 kkal
HigH20 = m * Cp * L\T = 134,2672 * 0,49 * ( 900 - 25) = 57567,0809 kkal
HigN2 = m * Cp * L\ T = 5790,6573 * 0,26 * ( 900 - 25 ) = 1317374,5350 kkal
Hig02 = m * Cp * dT = 1759,1870 * 0,245 * (900 - 25) = 377125,7189 kkal
Dari Smith Van Ness app.B
Tc N2 = 126,2 K
Pc N2= 34 attn
0) N2 = 0,0,038
Tc 02 = 154,6 K
Pc 02 = 50,43 attn
.0) 02 = 0,022
Tr N2 900 + 273 9,2948 126,2
PrN2 = 9.86 = 0 29 34 '
Tr 02 900+ 273 758 3 , 7 154,6
Pr 02 = 9.86 = 01955 50,43 '
Tc H2O = 647,1 K
Pc H2O = 220,5 attn
0) .H20 = 0,345
Tc NH3 = 405,7 K
Pc NH3 = 112,8 attn
0) NH3 = 0,253
TrH20= 900+273 1,8127 647,1
Pr H2O = 9,86 = 0 0447 220,5 '
900+273 Tr NH3 2,8913
154,6
Pr NH3 = 9.86 = 0195 50,43 '
B-15
AppendiksB
Dari Smith Van Ness app B:
(HR
)0 = 00039 RT N2 ,
c
(HRM2 = (( 0,0039 + (0,038. 0,0419) ). 8,314 . 126,2) / 4,2
= 1,3720 kkallkmol
= 1,3720 kkallkmol x 206,6092 kmol = 283,7503 kkal
(HR)02 = (( -0,0007 + (0,022. 0,0385) ). 8,314 . 154,6) / 4,2
= 0,045 kkallkmol
= 0,045 kkallkmol x 54,9746 kmol = 2,4731 kkal
(HR)H2o = (( -0,0149 + (0,345. 0,0011)).8,314.647,1) / 4,2
= -18,60 kkallkmol
= -18,60 kkallkmol x 7,3401 kmol = -138,7431 kkal
(HRMm = (( -0,0066 + (0,253.0,0122)).8,314.647,1) / 4,2
= -4,4278 kkallkmol
= -4,4278 kkallkmol x 25,1087 kmol = -111,175& kkal
. n ...... _ ... _ ...... _ .. n .. 1.. ... :1 .. A ..... _ '"'T: ..........
B-16
Appendiks B B-17
HN2 = HigN2 + (HR~2 = 1317374,5351 + 283,7503 = 1317658,2854 kkal
Ho2 = Hig02 + (HR)02 = 361732,8324 + 2,4731 361735,3056 kkal
HH20 = H igH20 + (HR
)H2o = 55217,4042 + -138,7431 55078,6611 kkal
HNH3 = HigNH3 + (HR~3 = 220360,6576 + -111,1758 = 220249.4818 kkal
Total panas masuk: =1962382,9908 kkal
Panas keluar :
Suhu gas keluar = 900°C
T 900+25 = 462 5 °C = 864 5 of 2 ' ,
Dari kern fig. 3 :
Cp NO = 0,255 Btu / lb of = 0,255 kkal / kg °C
Cp H20 = 0,51 Btu / Ib of = 0,49 kkal / kg °C
Cp N2 = 0,265 Btu / Ib of = 0,25 kkal / kg °C
Cp 02 = 0,25 Btu / lb OF = 0,265 kkal / kgoC
H igNO = m * Cp * ~T = 723,1320 * 0,255 * (900 - 25) = 161348,8205 kkal
H igH20 = m * Cp * ~T = 812,2035 * 0,51 * (900 - 25) = 362445,7962 kkal
HigN2 = m * Cp * ~T = 5804,7182 * 0,265 * (900 - 25) = 1345969,0319 kkal
H02 = m * Cp * ~T = 770,9067 * 0,25 * (900 - 25) = 168635,8340 kkal
Dari Smith Van Ness app.B
Tc N2 = 126,2 K Tc H2O = 647,1 K
Pc N2 = 34 atm Pc H2O = 220,5 atm
ro N2 = 0,0,038 ro H2O = 0,345
Appendiks 8
Tc 02 = 154,6 K
Pc 02 = 50,43 attn
0) 02 = 0,022
Tc NO = 180,2 K
Pc NO = 64,8 atm
0) NO = 0,583
Tr N2 900 + 273 9,2948 126,2
PrN2 = 9.37 = 0 29 34 '
·900+273 Tr02 7,5873
154,6
Pr 02 = 9.37 = 01955 50,43 '
Dari Smith Van Ness app B:
(HRi =00419 RT N2 ,
c
(HRi = 0 0385 RT 02 ,
c
Tc NH3 = 405,7 K
Pc NH3 = 112,8 attn
0) NH3 = 0,253
Tr H2O = 900 + 273 1,8127 647,1
Pr H20 = 9,37 = 0 0447 220,5 '
900+273 TrNO 6,5094
180,2
PrNO= 9.37 =01448 64 8 ' ,
(HRi = 00251 RT NO ,
c
8-18
AppendiksB
(HR)=( (HR)o +ro.(HRY ).R.Tc RTc RTc
(HR)N2 = « 0,0039 + (0,Q38. 0,0419) ). 8,314 . 126,2) 1 4,2
= 1,3720 kkallkmol
= 1,3720 kkallkmol x 207,3114 kmol = 284,4393 kkal
(HR)02 = « -0,0007 + (0,022. 0,0385) ). 8,314 . 154,6) 14,2
= 0,045 kkallkmol
= 0,045 kkallkmol x 24,0908 kmol = 1,0838 kkal
(HR}mO = « -0,0149 + (0,345.0,0011».8,314.647,1) 14,2
= -18,60 kkallkmol
= -18,60 kkallkmol x 45,1224 kmol = -839,2784 kkal
(HR~O = « 0,0123 + (0,583. 0,0251».8,314.180,2) 14,2
= 9,6074 kkallkmol
= 9,6074 kkallkmol x 24,1044 kmol ~ 231,5802 kkal
HN2 = HigN2 + (HR)N2 = 1345969,0319 + 284,4393 = 1325319,5423 kkal
Ho2 = Hig02 + (HR)02 = 168635,8340 + 1,0838 = 168636,9178 kkal
Hmo = Higmo + (HR)mo = 362445,7962 + -839,2784 = 361606,5178 kkal
HNO = HigNO + (HR)No = 161348,8205 + 231,5802 = 161580.4007 kkal
Total panas keluar = 2038077,3074 kkal
Panas masuk = panas keluar + panas reaksi + Q
1962382,9908 = 2038077,3074 - 1385185,5 + Q
Q = 1309491,1830 kkall jam = 5456213,2630 kj/kg
B-19
~A~pp~eillndillik~s~B~ ____________________________________________ ~B~-20
Kebutuhan steam :
Suhu steam masuk = 200°C
Dari Geankoplis, app.A. :
'A. steam = 1940,75 kj/kg
Q=m*'A.
5456213,2630 = 2811 3942 k 194075 ' g ,
Neraca panas:
Masuk kkal / jam Keluar
Panas masuk 1962382,9908 Panas keluar
Panas reaksi 1385185,5000 Panas diserap
Total 3347568,4900 Total
3. Heat Exchanger (E - 212 )
Udara , .. 30°C
Campuran gas d Oksidator I 900°C
an ... ...
Suhu gas masuk = 900°C
Heat Exchanger
~1l00 °C
T = 900 + 25 = 462 5 °C = 864 5 OF 2 ' ,
Prarencana Pabrik Asaro Nitrat
... ...
kkal/jam
2038077,3074
1309491,1830
3347568,4900
Campuran gas ke oksidator 2
200°C
AppendiksB
Dari Kern fig. 3 :
Cp NO = 0,255 Btu / Ib of = 0,255 kkal / kg °C
Cp H20 = 0,51 Btu / Ib of = 0,51 kkal / kg °C
Cp N2 = 0,265 Btu / lb of = 0,265 kkal / kg °C
Cp O2 = 0,25 Btu / lb of = 0,25 kkal / kg °C
HigNO = m * Cp * L1T = 723,1320 * 0,255 * (900 - 25) = 161348,8205 kkal
HigH20 = m * Cp * L1T = 812,2035 * 0,51 * (900 - 25) = 362445,7962 kkal
H;gN2 = m * Cp * L1T = 5804,7182 * 0,265 * (900 - 25) = 1345969,0319 kkal
H02 = m * Cp * L1T = 770,9067 * 0,25 * ( 900 - 25) = 168635,8340 kkal
Dari Smith Van Ness app.B
Tc N2 = 126,2 K
PcN2 =34 atm
0) N2 = 0,0,038
Tc 02 = 154,6 K
Pc 02 = 50,43 atm
0) 02 = 0,022
Tr N2 = 900 + 273 9,2948 126,2
PrN2 = 9.37 = 0 29 34 '
Tr 02 900 + 273 7,5873 154,6
Pr 02 = 9.37 = 0 1955 50,43 '
Tc H2O = 647,1 K
. Pc H2O = 220,5 atm
0) H2O = 0,345
Tc NO = 180,2 K
Pc NO = 64,8 atm
0) NO= 0,583
TrH20= 900+273 1,8127 647,1
Pr H2O = 9,37 = 0 0447 220,5 '
900+273 TrNO 6,5094
180,2
PrNO= 9.37 =01448 648 ' ,
B-21
Appendiks B
Dari Smith Van Ness app B:
(HR
)0 = 00039 RT N2 ,
c
(HR)l . = 00011 RT H2O ,
c
(HR~2 = (( 0,0039 + (0,038. 0,0419) ). 8,314. 126,2) / 4,2
= 1,3720 kkal/kmol
= 1,3720 kkal/kmol x 207,3114 kmol = 284,4393 kkal
(HR)02 = (( -0,0007 + (0,022. 0,0385) ). 8,314. 154,6) / 4,2
= 0,045 kkal/kmol
= 0,045 kkal/kmol x 24,0908 kmol = 1,0838 kkal
(HR)H20 = (( -0,0149 + (0,345.0,0011».8,314.647,1) / 4,2
= -18,60 kkallkmol
= -18,60 kkal/kmol x 45,1224 kmol = -839,2784 kkal
(HR~o = (( 0,0123 + (0,583. 0,0251».8,314 :180,2) / 4,2
= 9,6074 kkal/kmol
= 9,6074 kkal/kmol x 24,1044 kmol = 231,5802 kkal
B-22
Appendiks B B-23
HN2 = HigN2 + (HR~2 = 1345969,0319 + 284,4393 1325319,5423 kkal
H02 = Hig02 + CHR)02 = 168635,8340 + 1,0838 168636,9178 kkal
Hmo = Higmo + (HR)mo = 362445,7962 + -839,2784 = 361606,5178 kkal
HNO = HigNO + (HR~O = 161348,8205 + 231,5802 161580,4007 kkal
Total panas masuk: = 2038077,3074 kkal
Panas Keluar :
Suhu gas keluar = 200°C
T = 200 + 25 = 112 5 °C = 234 5 OF 2 ' ,
Dari Kern fig. 3 :
Cp NO = 0,235 Btu / Ib OF = 0,235 kkal / kg °C
Cp H20 = 0,455 Btu / Ib OF = 0,455 kkal / kg °C
Cp N2 = 0,255 Btu / Ib OF = 0,255 kkal / kg °C
Cp 02 = 0,225 Btu / Ib OF = 0,225 kkal / kg °C
HigNO = m * Cp * .1T = 723,1320 * 0,235 * (200 - 25) = 29738,8022 kkal
HigmO = m * Cp * .1T = 812,2035 * 0,455 * (200 - 25) = 64671,7009 kkal
HigN2 = m * Cp * .1T = 5804,7182 * 0,255 * (200 - 25) = 259035,5495kkal
Hig02 = m * Cp * .1T = 770,9067 * 0,225 * (200 - 25 ) = 30354,4501 kkal
Dari Smith Van Ness app.B
Te N2 = 126,2 K Te H2O = 647,1 K
PeN2 =34 atm Pe H2O = 220,5 atm
(j) N2 = 0,0,038 (j) H2O = 0,345
Te 02 = 154,6 K Te NO = 180,2 K
AppendiksB
Pc 02 = 50,43 atm
(002 = 0,022
Tr N2 200 + 273 3,1632 126,2
PrN2= 9.37 =029 34 '
Tr 02 - 200 + 273 3,0595 154,6
Pr 02 = 9.37 = 0 1955 50,43 '
Dari Smith Van Ness app B:
(HRy = 0 0271 RT 02 ,
c
Pc NO = 64,8 atm
(0 NO = 0,583
Tr H2O = 200 + 273 - 7310 6471 ' ,
Pr H2O = 9,37 = 0 0447 220,5 '
Tr NO = 200 + 273 - 2 6249 180,2 '
Pr NO = 9.37 = 01448 648 ' ,
(HR~2 = « .0,0162 + (0,038. 0,0434) ). 8,314 . 126,2) / 4,2
= ·3,6350 kkallkmol
= ·3,6350 kkallkmol x 207,3114 kInol = -753,5812 kkal
B·24
AppendiksB
(HR)02 = « -0,0204 + (0,022.0,0271».8,314.154,6) / 4,2
= -6,0606 kkallkmol
= -6,0606 kkal/kmol x 24,0908 kmol = -146,0060 kkal
(HR)mo = « -0,0789 + 0,345. (-0,1343».8,314.647,1) / 4,2
= -160,4178 kkallkmol
= -160,4178 kkallkmol x 45,1224 kmol = -7238,4400 kkal
(HR~o = « -0,0227 + (0,583. 0,0092) ). 8,314.180,2) /4,2
= -6,1841 kkallkmol
= -6,1841 kkal/kmol x 24,1044 kmol = -149,0633 kkal
HN2 = HigN2 + (HR~2 = 259035,5495 - 753,5812
Ho2 = Hig02 + (HR)oz = 30354,4501- 146,0060
258281,9683 kkal
= 30208,4442 kkal
Hmo = HigH20 + (HR)mo = 64671,7009 -7238,4400 = 57433,2609 kkal
HNO = HigNO + (HR~o = 29738,8022 - 149,0633 29589.7389 kkal
Total panas keluar 375513,4122 kkal
Panas yang hilang = 5 % dari panas masuk:
= 0,05 * 2038077,3074
= 101903,8654 kkal / jam
Panas masuk: = panas keluar + panas hi lang + Q
2038077,3074 = 375513,4122 + 101903,8654 + Q
Q = 1560660,0298 kkal / jam
Kebutuhan udara :
T= 30+200 =115 0C=239 0P 2
B-25
Allllendiks B
Dari Kern fig. 3 :
Cp udara = 0,25 Bbtu / lb OF = 0,25 kkal / kg °C
Q=m*Cp*~T
m=-Q=-Cp*~T
= 1560660,0298 = 367214125 k / 'am 0,25 * (200 _ 30) , g J
Neraca Panas :
Masuk kkal / jam Keluar
Panasmasuk 2038077,3074 Panas keluar
Panas hilang
Panas diserap
Total 2038077,3074
4. Oksidator 2 ( R - 230 )
udara ~, 30°C
. Oksidator2
kkal / jam ..
375513,4122
101903,8654
1560660,0298
2038077,3074
recycle 200°C Campuran gas dr 200°C
HE .
1200 0 c
.. ~; ampuran gas ke kondenser
200°C
Reaksi: NO + .!. O2 2
MI = -27,3 kkal / mol
NO yang bereaksi = 27,9151 kmol = 27915,1 mol
MIr = -27,3 * 27915,1 = -762081,5341 kkal / jam
Prarencana Pahrik Asam Nitrat
B-26
~A~pp~en~d~ik~s~B ____________________________________________ ~B~-27
Panas masuk :
Suhu gas masuk = 200°C
T = 200 + 25 = 112 5 °C = 385 5 oK = 234 5 of 2 ' ) ,
Daribahan:
Dari Kern fig. 3 :
Cp NO = 0,235 Btu / Ib of = 0,235 kkal / kg °C
Cp H20 = 0,455 Btu / Ib OF = 0,455 kkal / kg °C
Cp N2 = 0,255 Btu / Ib OF = 0,255 kkal / kg °C
Cp O2 = 0,225 Btu / Ib OF = 0,225 kkal / kg °C
Massa total NO masuk = 881,5287 kg/jam = 29,3843 kmol/jam
Massa total N2 masuk = 11609,4364 kg/jam =414,6227 kmol/jam
Massa total 02 masuk = 1095,7442 kg/jam = 34,2420 kmol/jam
Massa total H2O masuk = 812,2035 kg/jam = 45,1224 kmol/jam
Massa total N02 masuk = 32,8833 kg/jam 7' 0,8221 kmol/jam
HigNO = m * Cp * ~T = 881,5287 * 0,235 * (200 - 25) = 36252,8665 kkal
HigN02 = m * Cp * ~T = 32,8833 * O,Qll * (200 - 25 ) 63,3004 kkal
HigH20 = m * Cp * ~T = 812,2035 * 0,455 * (200 - 25 ) 64671,7009 kkal
HigN2 = m * Cp * ~T = 11609,4364 * 0,255 * (200 - 25) = 518071,0992 kkaI
Hig02 = m * Cp * ~T = 1095,7442 * 0,225 * (200 - 25) = 43144,9267 kkal
Dari Smith Van Ness app.B
Tc N2 = 126,2 K TcH20 = 647;1 K
PcN2 =34 atm Pc H2O = 220,5 atm
Prarencana Pabrik Asam Nitrat
AppendiksB
0) N2 = 0,0,038
Tc 02 = 154,6 K
Pc 02 = 50,43 atm
0) 02 =0,022
Tc N02 = 309,6 K
Pc N02 = 72,45 atm
0) N02 = 0,141
TrN2 200+273 3,1632 126,2
PrN2 = 9.37 = 0 29 34 '
Tr 02 200 + 273 3,0595 154,6
Pr 02 = 9.37 = 01955 50,43 '
Tr N02 = 200 + 273 1,5278 309,6
PrN02 = 9.37 = 12473 72,45 '
Dari Smith Van Ness app B:
0) H2O = 0,345
Tc NO = 180,2 K
Pc NO = 64,8 atm
0) NO = 0,583
Tr H2O = 200 + 273 ,7310 647,1
Pr H2O = 9,37 = 00447 220,5 '
Tr NO = 200 + 273 2,6249 180,2
Pr NO = 9.37 = 01448 64 8 ' ,
(HRi -'----'- H2O = -0 1343
RT ' c
B-28
AppendiksB
(HR
)1 = 0 0092 RT NO ,
c
(HR~2 = (( -0,0162 + (0,038.0,0434)).8,314. 126,2) 14,2
= -3,6350 kkallkmol
= -3,6350 kkallkmol x 414,6227 kInol = -1507,1624 kkal
. (HR)m = (( -0,0204 + (0,022. 0,0271) ). 8,314 . 154,6) 14,2
= -6,0606 kkallkmol
= -6,0606 kkallkmol x 34,2420 kInol = -207,5286 kkal
(HR)H2o = (( -0,0789 + 0,345. (-0,1343)).8,314.647,1) 14,2
= -160,4178 kkallkmol
= -160,4178 kkallkmol x 45,1224 kInol = -7238,4400 kkal
(HR~O = (( -0,0227 + (0,583. 0,0092) ). 8,314 .180,2 ) 14,2
= -6,1841 kkalIkmol
= -6,1841 kkallkmol x 29,3843 kInol = -181,7145 kkal
(HR~02 = (( -0,0605 + (0,141. -0,0097) ). 8,314 .180,2 ) 1 4,2
== -37,9163 kkallkmol
= -37,9163 kkallkmol x 0,8221 kInol = -31,1703 kkal
Prarencana Pahrik Asam Nitrat
B-29
Appendiks B B-30
HN2 = HigN2 + (HR
hJ2 = 518071,0992 - 1507,1624 = 516563,9368 kkal
H02 = Hig02 + (HR)02 = 43144,9267 - 207,5286 42937,3981 kkal
Hmo = HigmO + (HR)mo =64671,7009 -7238,4400 = 57433,2609 kkal
HNO = H igNO + (HRhJo = 36252,8665 - 181,7145
H N02 = HigN02 + (HR
hJ02 = 63,3004 - 31,1703
Total panas masuk:
Panas keluar :
Suhu gas keluar pada suhu = 200°C
T = 200 + 25 = 112 5 °C = 234 5 OF 2 ' ,
Dari Kern fig. 3 :
Cp NO = 0,235 Btu / lb OF = 0,235 kkill / kg °C
Cp H20 = 0,455 Btu / lb OF = 0,455 kkal / kg °C
Cp N02 = O,QIl Btu / lb OF = O,QII kkal / kg °C
Cp N2 = 0,255 Btu / lb OF = 0,255 kkal / kg °C
Cp O2 = 0,225 Btu / lb OF = 0,225 kkal / kg °C
36071,1520 kkal
32,1300 kkal
= 653037,8777 kkal
HigNO = m • Cp • t1T = 44,0764 • 0,235 • (200 ~ 25 ) 1812,6433 kkal
H igN02 = m • Cp· t1T = 1316,9767· 0,011 • (200 - 25) = 2535,1802 kkaI
HigH20 = m • Cp • t1T = 812,2035 • 0,455 • (200 - 25) = 64671,7009 kkal
H igN2 = m • Cp· t1T = 11609,4364 • 0,255 • (200 - 25) = 518071,0992 kkal
Hig02 = m • Cp ... t1T = 649,1030 ... 0,225 ... (200 - 25) = 25558,4298 kkal
AppendiksB
Dari Smith Van Ness app.B
Tc N2 = 126,2 K
Pc N2 = 34 atm
co N2 = 0,0,038
Tc 02 = 154,6 K
Pc 02 = 50,43 atm
co 02 = 0,022
Tc N02 = 309,6 K
Pc N02 = 72,45 atm
co N02 = 0,141
TrN2 200+273 3,1632 126,2
Pr N2 = 9.37 = 0 29 34 '
200+273 Tr02 3,0595
154,6
Pr 02 = 9.37 = 0 1955 50,43 '
Tr N02 200 + 273 1,5278 309,6
Pr N02 = 9.37 = 1 2473 72,45 '
Dari Smith Van Ness app B:
Tc H2O = 647,1 K
Pc H2O = 220,5 atm
co H2O = 0,345
Tc NO = 180,2 K
Pc NO = 64,8 atm
co NO = 0,583
TrH20= 200+273 ,7310 647,1
Pr H2O = 9,37 = 0 0447 220,5 '
Tr NO = 200 + 273 2,6249 180,2
Pr NO = 9.37 = 0 1448 648 ' ,
B-3l
AppendiksB
(HRy =00271 RT 02 ,
c
(HRy =00092 RT NO ,
c
(HR)N2 = (( -0,0162 + (0,038. 0,0434) ). 8,314 . 126,2) / 4,2
= -3,6350 kkallkmol
= -3,6350 kkallkmol x 414,6227 kmol = -1507,1624 kkal
. (HR)02 = (( -0,0204 + (0,022. 0,0271) ). 8,314 . 154,6) / 4,2
= -6,0606 kkallkmol
= -6,0606 kkallkmol x 28,6299 kmol = -122,9369 kkal
(HR)H2o = (( -0,0789 + 0,345. (-0,1343)).8,314.647,1) / 4,2
= -160,4178 kkallkmol
= -160,4178 kkallkmol x 45,1224 kmol = -7238,4400 kkal
(HR)No = (( -0,0227 + (0,583. 0,0092) ). 8,314.180,2) / 4,2
= -6,1841 kkalIkmol
= -6,1841 kkallkmol x 1,4692 kmol = -9,0857 kkal
Prarencana Pabrik Asaro Nitrat
B-32
AppendiksB
(HR~02 = « -0,0605 + (0,141. -0,0097) ). 8,314 .180,2 ) /4,2
= -37,9163 kkallkrnoI
= -37,9163 kkallkrnol x 28,6299 kInol = -1085,5402 kkal
HN2 = HigN2 + (HR~2 = 518071,0992 - 1507,1624 = 516563,9368 kkal
H02 = Hig02 + (HR)02 = 25558,4298 - 122,9369 25435,4928 kkal
HH20 = HigH20 + (HR
)H2o =64671,7009 -7238,4400 = 57433,2609 kkal
HNO = HigNO + (HR~O = 1812,6433 - 9,0857 1803,5576 kkal
HN02 = HigN02 + (HR~02 = 2535,1802 - 1085,5402 1449,6400 kkal
Total panas keluar = 602685,8880 kkal
Panas masuk = panas keluar + panas reaksi + Q
653037,8777 = 602685,8880 -762081,5341 + Q
Q = 812433,5238 kkal/ jam
Kebutuhan udara sebagai pendingin :
m= Q Cp* I1T
m = 812433,5238 = 19116 0829 k / ·am 0,25 * (200 - 30) , g J
Neraca panas:
Masuk kkal / jam Keluar
Panasmasuk 653037,8777 Panas keluar
Panas reaksi 762081,5341 Panas diserap
Total 1415119,4118
kkal / jam
602685,8880
812433,5238
1415119,4118
B-33
AppendiksB
5. Kondenser(E-231)
I Air pendingin .. 28°C
Campuran gas ,----....!--, Campuran gas Dari oksidator 2 --~.. kondensor ke absorber r
200°C 40°C
Dari GeankopJis tab. A.2-9 :
Panas laten kondensasi ( ')..) = 2406,73 kj / kg
= 575,22 kkal / kg
H20 yang mengembun = 727,2250 kg / jam
Panas kondensasi = 727,2250 * 575,22 = 418314,3549 kkal
Suhu gas masuk pada suhu = 200°C
T = 210 + 25 117 5 °c = 243 5 OF 2 ' ,
Dari Kern fig. 3 :
Cp NO = 0,235 Btu / Ib OF = 0,235 kkall kg °c
Cp H20 = 0,455 Btu / lb OF = 0,455 kkal / kg °c
Cp N02 = 0,011 kkall mol OK
Cp N2 = 0,255 Btu / Ib OF = 0,255 kkal / kg °c
Cp O2 = 0,225 Btu / lb OF = 0,225 kkal / kg °c
HigNO = m * Cp * AT = 44,0764 * 0,235 * ( 200 - 25) = 1812,6433 kkal
HigN02 = m * Cp * AT = 1316,9767 * 0,011 * (200 - 25) = 2535,1802 kkal
HigH20 = m * Cp * AT = 812,2035 * 0,455 * (200 - 25) = 64671,7009 kkal
B-34
AppendiksH
HigN2 = m * Cp * dT = 11609,4364 * 0,255 * (200 - 25) = 518071,0992 kkal
Hig02 = m * Cp * dT = 649,1030 * 0,225 * (200 - 25) = 25558,4298 kkal
Dari Smith Van Ness app.B
Tc N2 = 126,2 K
PcN2 =34 atm
(i) N2 = 0,0,038
Tc 02 = 154,6 K
Pc 02 = 50,43 atm
(i) 02 = 0,022
Tc N02 = 309,6 K
Pc N02 = 72,45 atm
(i) N02 = 0,141
200+273 TrN2 3,1632
126,2
PrN2 = 9.37 = 0 29 34 '
Tr 02 = 200 + 273 3,0595 154,6
Pr 02 = 9.37 = 0 1955 50,43 '
Tr N02 = 200 + 273 1,5278 309,6
Pr N02 = 9.37 = 1 2473 72,45 '
Tc H2O = 647,1 K
Pc H2O = 220,5 atm
(i) H2O = 0,345
Tc NO = 180,2 K
Pc NO = 64,8 atm
(i) NO = 0,583
TrH20= 200+273 ,7310 647,1
Pr H2O = 9,37 = 0 0447 220,5 '
200+273 TrNO 2,6249
180,2
PrNO= 9.37 =01448 64 8 ' ,
B-35
AppendiksB
Dari Smith Van Ness app B:
(HRi =00434 RT N2 ,
c
(HRi -'---'-H2O = -0 1343
RT ' c
(HRi = 0 0271 RT 02 ,
c
(HRi -'---'- NO = -0 0097
RT ' c
(HR~2 = « -0,0162 + (0,038. 0,0434) ).8,314. 126,2) / 4,2
= -3,6350 kkal/kmol
= -3,6350 kkal/kmol x 414,6227 lanol = -1507,1624 kkal
(HR)02 = (( -0,0204 + (0,022.0,0271) ). 8,314. 154,6) / 4,2
= -6,0606 kkailkmol
= -6,0606 kkal/kmol x 28,6299 lanol = -122,9369 kkal
(HR)H2o = « -0,0789 + 0,345. (-0,1343) ).8,314.647,1) /4,2
= -160,4178 kkal/kmol
Pr~r,.anrgn ... p ... hrl1r A ,:!gm 1\Titrgt
B-36
AppendiksB
(HR)No = « -0,0227 + (0,583. 0,0092) ). 8,314 .180,2 ) / 4,2
= -6,1841 kkallkmol
= -6,1841 kkallkmol x 1,4692 kInol = -9,0857 kkal
(HR)N02 = « -0,0605 + (0,141. -0,0097) ). 8,314.180,2 ) / 4,2
= -37,9163 kkallkmol
= -37,9163 kkallkmol x 28,6299 kInol = -1085,5402 kkal
HN2 = HigN2 + (HR)N2 = 518071,0992 - 1507,1624 = 516563,9368 kkal
Ha2 = Hi~02 + (HR)02 = 25558,4298 - 122,9369 25435,4928 kkal
HHlO = HigH20 + (HR)mO = 64671,7009 - 7238,4400 = 57433,2609 kkal
HNO = HigNO + (HR)No = 1812,6433 - 9,0857 1803,5576 kkal
HN02 = HigN02 + (HR)N02 = 2535,1802 - 1085,5402 1449,6400 kkal
Total panas masuk = 602685,8880 kkal
Suhu gas keluar pada suhu = 40°C
T = 40 + 25 = 3250C = 9050F 2 ' ,
Dari Kern fig. 3 :
Cp NO = 0,23 Btu / lb OF = 0,23 kkal / kg ClC
Cp H20 = 0,45 Btu / lb OF = 0,45 kkal / kg °C
Cp N02 = 5,0901.10-3 kkal / mol °C
Cp N2 = 0,25 Btu / lb OF = 0,25 kkal / kg °C
Cp 02 = 0,22 Btu / lb OF = 0,22 kkal / kg °C
HigNO = m * Cp * dT = 44,0764 * 0,235 * ( 40 - 25) 1,4692 ~l
HigN02 = m * Cp * d T = 1316,9767 * 0,0051 * ( 40 - 25 ) = 100,7000 kkal
B-37
AppendiksB
HigH20 = m * Cp * ~T = 84,9785 * 0,45 * ( 40 - 25 ) 573,6049 kkal
HigN2 = m * Cp * ~T = 11609,4364 * 0,255 * (40 - 25) = 43535,3865 kkal
Hig02 = m * Cp * ~T = 649,1030 * 0,225 * ( 40 - 25) = 2142,0398 kkal
HH20liq = m * Cp * ~T = 727,2250 * 1 * ( 40 - 25) = 10908,3750 kkal
Dari Smith Van Ness app.B
Tc N2 = 126,2 K
PcN2 =34 atm
0) N2 = 0,0,038
Tc 02 = 154,6 K
Pc 02 = 50,43 atm
0) 02 = 0,022
Tc N02 = 309,6 K
Pc N02 = 72,45 atm
0) N02 = 0,141
Tr N2 = 40 + 273 2,4802 126,2
PrN2 = 9.37 = 0 29 34 '
Tr 02 = 40 + 273 2,0246 154,6
Pr 02 = 9.37 = 0 1955 50,43 '
Tr N02 40 + 273
1,0110 309,6
Tc H2O = 647,1 K
Pc H2O = 220,5 atm
0) H2O = 0,345
Tc NO = 180,2 K
Pc NO = 64,8 atm
0) NO =0,583
Tr H2O = 200+273 ,7310 647,1
Pr H2O = 9,37 = 0 0447 220,5 '
TrNO= 40+273 1,7370 180,2
Pr NO = 9.37 = 01448 648 ' ,
B-38
AppendiksB
Pr N02 = 9.37 = 1 2473 72,45 '
Dari Smith Van Ness app B:
(HR)o ..:....R-T~NO = -0,0528
c
(HRi = 0 0139 RT 02 ,
c
(HRi = 0 0019 RT NO ,
c
(HR)! .o...--'-NO = -0 1165
RT ' c
(HR~2 = « -0,0491 + (0,038. 0,0336) ). 8,314. 126,2) / 4,2
= -11,9470 kkallkmol
= -11,9470 kkallkmol x 414,6227 kmol = -4953,4961 kkal
(HR)02 = « -0,0427 + (0,022. 0,0139) ). 8,314 . 154,6) / 4,2
= -12,9741 kkallkmol
= -12,9741 kkallkmol x 20,2845 kmol = -263,1724 kkal
(HR)H2o = « -0,5512 + 0,345. (-0,8869)).8,314.647,1) / 4,2
= -1098,0052 kkallkmol
Prarencana Pabrik Asam Nitrat
B-39
AppendiksB
= -1098,0052 kkaIlkmol x 4,7210 kInol = -5183,7121 kkal
(HR~o = « -0,0528 + (0,583. 0,0019) ). 8,314 .180,2 ) /4,2
= -18,4392 kkaIlkmol
= -18,4392 kkaIlkmol x 1,4692 kInol = -27,0911 kkal
(HR~02 = « -0,1324 + (0,141. -0,1165)). 8,314.180,2) /4,2
= -91,2099 kkallkmol
= -91,2099 kkaIlkmol x 28,6299 kInol = -2611,3328 kkal
HN2 = Hig.N2 + (HR~2 = 43535,3865 - 4953,4961 = 516563,9368 kkal
Ho2 = Hig.02 + (HR)02 = 2142,0398 - 263,1724 1878,8675 kkal
HH20 = HigH20 + (HR)H2o = 573,6048 - 5183,7121 -4610,1074 kkal
HNO = HigNO + (HR~o = 152,0637 - 27,0911 124,9726 kkal
HN02 = HigN02 + (HR~02 = 100,7487 - 2611,3328 = 1449,6400 kkal
HH20liq = 10908,3750 kkal
Total panas keluar = 44373,4141 kkal
Panas masuk: = panas keluar + panas pengembunan + Q
602685,8880 = 44373,4141 + 418314,3549 + Q
Q = 139998,1190 kkal
Kebutuhan air pendingin :
C; air = 1 kkal / kg °C
m=-=QC */)"T p
139998,1190
1 * (38 - 28)
m=59171,1071 kg/jam
PrRren(,.IInA P'Ihrik A~Rm Nitrat
B-40
AppendiksB B-41
Neraca panas :
Masuk kkal / jam Keluar kkal / jam
Panas total 602685,8880 Panas total 44373,4141
Panas pengembunan 418314,3549
Panas diserap 139998,1190
Total 602685,8880 602685,8880
6. Absorber ( D - 240 )
Gas buang .~
HN~ Jiq
MI = -32,4 kkal / mol
Panas reaksi :
Hr = -32,4 * 1000 * 27,1984
Hr = -881229,2102 kkal / jam
Panas masuk :
Suhu gas masuk pada suhu = 40 °C
PrllrenCllna P"hrik ASllm Nitrat
AppendiksB B-42
T = 40 + 25 = 3250C = 9050F 2 ' ,
Dari Kern fig. 3 :
Cp NO = 0,23 Btu / lb of = 0,23 kkal / kg °C
Cp H20 = 0,45 Btu / lb OF = 0,45 kkal / kg °C
Cp N02 = 0,0051 Btu / lb of = 0,0051 kkal / kg °C
Cp N2 = 0,25 Btu / lb of = 0,25 kkal / kg °C
Cp O2 = 0,22 Btu / lb of = 0,22 kkal / kg °C
HigNo = m * Cp * i1 T = 44,0764 * 0,235 * ( 40 - 25 ) 1,4692 kkal
HigN02 = m * Cp * i1T = 1316,9767 * 0,0051 * (40 - 25) = 100,7000 kkal
HigH20 = m * Cp * i1T = 84,9785 * 0,45 * ( 40 - 25) 573,6049 kkal
HigN2 = m * Cp * i1T = 11609,4364 * 0,255 * (40 - 25) = 43535,3865 kkal
Hig02 = m * Cp* i1T = 649,1030 * 0,225 * ( 40 - 25) = 2142,0398 kkal
Dari Smith Van Ness app.B
Tc N2 = 126,2 K Tc H2O = 647,1 K
Pc N2 = 34 atm Pc H2O = 220,5 atm
ill N2 = 0,0,038 ill H2O = 0,345
Tc 02 = 154,6 K Tc NO = 180,2 K
Pc 02 = 50,43 atm Pc NO = 64,8 atm
ill 02 = 0,022 ill NO = 0,583
Tc N02 = 309,6 K
Pc N02 = 72,45 atm
ill N02 = 0,141
Prarencana Pabrik Asam Nitrat
· Ap'pendiks B
Tr N2 40 + 273 2,4802 126,2
PrN2 = 9.37 = 0 29 34 '
Tr 02 40 + 273 2,0246 154,6
Pr 02 = 9.37 = 0 1955 50,43 '
TrN02 40+273 1,0110 309,6
Pr N02 =' 9.37 = 1 2473 72,45 '
Dari Smith Van Ness app B:
(HRi =00l39 RT 02 ,
c
(HR)o -'--~N02 = -0, l324
RTc
Prarencana Pabrik Asarn Nitrat
TrH20= 200+273 ,7310 647,1
Pr H2O = 9,37 = 0 0447 220,5 '
Tr NO = 40 + 273 1,7370 180,2
Pr NO = 9.37 = 0 1448 648 ' ,
(HR)l -'----'- H2O = -0 8869
RT ' c
(HRi =00019 RT NO ,
c
B-43
~Ap~p~en~d~ik~sB~ ________________________________________ ~B~44
(HR~2 = (( -0,0491 + (0,038.0,0336».8,314. 126,2) 14,2
= -11,9470 kkallkmol
= -11,9470 kkallkmol x 414,6227 kmol = -4953,4961 kkal
(HR)02 = (( -0,0427 + (0,022. 0,0139) ). 8,314 . 154,6) 14,2
= -12,9741 kkallkmol
= -12,9741 kkallkmol x 20,2845 kmol = -263,1724 kkal
(HR)H20 = (( -0,5512 + 0,345. (-0,8869».8,314.647,1) 14,2
= -1098,0052 kkallkmol
= -1098,0052 kkallkmol x 4,7210 kmol = -5183,7121 kkal
(if~o = « -0,0528 + (0,583.0,0019) ). 8,314.180,2) 14,2
= -18,4392 kkallkmol
= -18,4392 kkallkmol x 1,4692 kmol = -27,0911 kkal
(HR~02 =(( -0,1324+ (0,141. -0,1165)). 8,314.180,2)/4,2
= -91,2099 kkallkmol
= -91,2099 kkallkmol x 28,6299 kmol = -2611,3328 kkal
HN2 = HigN2 + (HR~2 = 43535,3865 - 4953,4961 = 516563,9368 kkal
H02 = Hig02 + (HR)o2 = 2142,0398 - 263,1724
HH20 = HigH20 + (HR)H2o = 573,6048 - 5183,7121
HNO = HigNO + (HR~o = 152,0637 - 27,0911
HN02 = HigN02 + (HR)oo2 = 100,7487 - 2611,3328
Total panas masuk
Panas keluar :
1878,8675 kkal
-4610,1074 kkal
124,9726 kkal
= 1449,6400 kkal
= 33465,0391 kkal
~M~p~en~d~ik~s~B ____________________________________________ ~B~45
Suhu gas keluar pada suhu = 40°C
T = 40 + 25 = 3250C = 9050F 2 ' ,
Dari Kirk & Othmer tab. 1:
Cp HN03 = 0,58 kaI / gr °C
Dari Kern fig. 3 :
Cp NO = 0,23 Btu / lb of = 0,23 kkal / kg °C
Cp HzO = 0,45 Btu / Ib of = 0,45 kkal / kg °C
Cp N02 = 0,0051 Btu / lb "F = 0,0051 kkal / kg °C
Cp Nz = 0,25 Btu / Ib of = 0,25 kkaI / kg °C
Cp Oz = 0,22 Btu / Ib °F= 0,22 kkaI lkg °C
HigNO = m * Cp * ~T = 316,0608 * 0,235 * (40 - 25) = 1090,4096 kkaI
HigNOZ = m * Cp * ~T = 65,8488 * 0,0051 * ( 40 - 25) = 5,0374 kkaI
HigNZ = m * Cp * ~T = 11609,4364 * 0,255 * (40 - 25) = 43535,3865 kkaI
Hig02 = m * Cp * ~T = 649,1030 * 0,225 * ( 40 - 25) = 2142,0398 kkaI
HH20liq = m * Cp * ~T = 761,5561 * 1 * ( 40 - 25) = 11423,3416 kkaI
HHN03 = m * Cp * ~T = 1142,3342 * 0,5 * ( 40 - 25) = 8567,5062 kkal
Dari Smith Van Ness app.B
Tc N2 = 126,2 K Tc N02 = 309,6 K
PcN2 =34 atm Pc N02 = 72,45 atm
0) N2 = 0,0,038 0) N02 = 0,141
Tc 02 = 154,6 K Tc NO = 180,2 K
Pc 02 = 50,43 atm Pc NO = 64,8 atm
Prarencana Pabrik Asam Nitrat
aAp~p~en~dl~·k~sB~ ________________________________________ ~B~46
0) 02 = 0,022
Tr N2 40 + 273 2,4802 126,2
PrN2 = 9.37 = 0 29 34 '
40+273 Tr02 2,0246
154,6
Pr 02 = 9.37 = 01955 50,43 '
Dari Smith Van Ness app B:
0) NO = 0,583
TrN02 40+273 1,0110 309,6
PrN02 = 9.37 = 12473 72,45 '
TrNO= 40+273 1,7370 180,2
PrNO = 9.37 = 01448 64 8 ' ,
(HR~2 = « -0,0491 + (0,038. 0,0336) ). 8,314. 126,2) / 4,2
= -11,9470 kkal/kmol
= -11,9470 kkal/kmol x 414,6227 kmol = -4953,4961 kkal
Prarencana Pabrik Asam Nitrat
A!1!1endiks B
(HR)02 = « -0,0427 + (0,022.0,0139)).8,314. 154,6)! 4,2
= -12,9741 kkallkmol
= -12,9741 kkallkmol x 20,2845 kmol = -263,1724 kkal
(HR)NO = « -0,0528 + (0,583. 0,0019) ).8,314 .180,2 ) / 4,2
= -18,4392 kkallkmol
= -18,4392 kkallkmol x 1,4692 kmol = -27,0911 kkal
(HR~02 = « -0,1324 + (0,141. -0,1165)). 8,314 .180,2)! 4,2
= -91,2099 kkallkmol
= -91,2099 kkallkmol x 1,4315 kmol = -130,5666 kkal
HN2 = HigN2 + (HR~2 = 43535,3865 - 4953,4961
Ha2 = Hig02 + (HR)o2 = 2142,0398 - 263,1724
HNO = HigNo + (HR~o = 152,0637 - 27,0911
HN02 = HigN02 + (HR~02 = 5,0374 - 130,5666
HNH03
HH20liq
Total panas keluar
Panas masuk = panas keluar + panas reaksi + Q
33465,0391 = 61222,2228 - 881229,2102 + Q
Q = 853472,0264 kkal / jam
= 516563,9368 kkal
1878,8675 kkal
124,9726 kkal
-125,5292 kkal
8567,5062 kkal
= 11423,3416 kkal
= 61222,2228 kkal
B-47
· MpendiksB
Neraca panas:
Masuk kkall jam Keluar kkall jam
Panas bahan 33465,0391 Panas bahan 61222,2228
Panas reaksi 880129,0154 Panas diserap 853472,0264
Total 913594,0545 913594,0545
7. Heater ( E - 232 )
Campuran gas recycle Dari gas buang --~. 40°C
heater Campuran gas recycle
1---.:' ke oksidator 2 200°C
.I. 48°C
Panas masuk :
Suhu masuk = 40°C
T = 40 + 25 = 3250C = 9050F 2 ' ,
Dari Kern fig. 3 :
Cp NO = 0,23 Btu lIb OF = 0,23 kkal / kg °C
Cp NOz = 0,0051 Btu / lb OP = 0,0051 kkal / kg °C
Cp Nz = 0,25 Btu / lb OF = 0,25 kkal / kg °C
Cp Oz = 0,22 Btu / lb of = 0,22 kkal / kg °C
HigNO = m * Cp * dT = 316,0608 * 0,235 * (40 - 25) = 1090,4096 kkal
HigN02 = m * Cp * dT = 65,8488 * 0,0051 * ( 40 - 25) 5,0374 kkal
Prarencana Pabrik Asam Nitrat
B-48
AppendiksB
HigN2 = m * Cp * L\T = 11609,4364 * 0,255 * (40 - 25) = 43535,3865 kkal
Hig02 = m * Cp * L\T = 649,1030 * 0,225 * ( 40 - 25) = 2142,0398 kkal
Dari Smith Van Ness app.B
Tc N2 = 126,2 K
PcN2 =34 atm
0) N2 = 0,0,038
Tc 02 = 154,6 K
Pc 02 = 50,43 atm
0) 02 = 0,022
Tr N2 40 + 273 2,4802 126,2
PrN2 = 9.37 = 0 29 34 '
Tr 02 40 + 273 2,0246 154,6
Pr 02 = 9.37 = 0 1955 50,43 '
Dari Smith Van Ness app B:
(HR
)' = 0 0336 RT N2 ,
c
Prarencana Pabrik Asam Nitrat
Tc N02 = 309,6 K
Pc N02 = 72,45 atm
0) N02 = 0,141
Tc NO = 180,2 K
Pc NO = 64,8 atm
0) NO = 0,583
TrN02 = 40+273 1,0110 309,6
Pr N02 = 9.37 = 1 2473 72,45 '
Tr NO = 40 + 273 1,7370 180,2
PrNO = 9.37 = 01448 648 ' ,
B-49
Ap,pendiks B
(HR)N2 = « -0,0491 + (0,038. 0,0336) ). 8,314 . 126,2) /4,2
= -11,9470 kkallkmol
= -11,9470 kkallkmol x 414,6227 kmol = -4953,4961 kkal
(HR)02 = « -0,0427 + (0,022.0,0139) ). 8,314. 154,6) /4,2
= -12,9741 kkallkmol
= -12,9741 kkallkmol x 20,2845 kmol = -263,1724 kkal
(HR)NO= « -0,0528 + (0,583. 0,0019)).8,314.180,2 )/4,2
= -18,4392 kkallkmol
= -18,4392 kkallkmoI x 1,4692 kmoI = -27,0911 kkaI
(HR)N02 = « -0,1324 + (0,141. -0,1165) ). 8,314 .180,2 ) /4,2
= -91,2099 kkaIlkmoI
= -91,2099 kkallkmol x 1,4315 kmol = -130,5666 kkal
HN2 = HigN2 + (HR)N2 = 43535,3865 - 4953,4961 = 516563,9368 kkal
Ha2 = Hig02 + (HR)02 = 2142,0398 - 263,1724 1878,8675 kkal
HNO = HigNO + (HR)No = 152,0637 - 27,0911 124,9726 kkal
HN02 = HigN02 + (HR)N02 = 5,0374 - 130,5666 -125.5292 kkal
Total panas masuk = 518442,2477 kkal
Panas keluar :
Suhu keluar pada = 200°C
B-50
AppendiksB
T= 200+25 11250C=23450F 2 ' ,
Dari Kern fig. 3 :
Cp NO = 0,235 Btu / Ib of = 0,235 kkal / kg °C
Cp NOz = 0,0104 Btu / Ib ~ = 0,0104 kkal / kg °C
Cp N2 = 0,25 Btu lIb OF = 0,25 kkal / kg °C
Cp Oz = 0,225 Btu / Ib of = 0,225 kkal / kg °C
RgNO = m * Cp * ~T = 316,0608 * 0,235 * (200 - 25) = 12721,4455 kkal
HigN02 = m * Cp * ~T = 65,8488 * 0,0051 * (200 - 25) = 58,7701 kkal
HigNZ = m * Cp * ~T = 11609,4364 * 0,255 * (200 - 25) = 507912,8424 kkal
HigOZ = m * Cp * ~T = 649,1030 * 0,225 * (200 - 25) = 24990,4646 kkal
Dari Smith Van Ness app.B
Te N2 = 126,2 K
PeN2 =34 atm
ill N2 = 0,0,038
Te 02 = 154,6 K
Pe 02 = 50,43 atm
ill 02 = 0,022
TrN2 200+273 3,1632 126,2
9.5 PrN2= -=029
34 '
Tr 02 200 + 273 1,7659 154,6
Te N02 = 309,6 K
Pe N02 = 72,45 atm
ill N02 = 0,141
Te NO = 180,2 K
Pe NO = 64,8 atm
ill NO =0,583
Tr N02 200 + 273 - 1 5278 309,6 '
Pr N02 = ~= 1 2473 72,45 '
Tr NO = 200 + 273 1,5150 180,2
B-51
Appendiks B
9.5 Pr02= --=0 1955
50,43 ' PrNO= 9.5 =01448
64 8 ' ,
Dari Smith Van Ness app B:
(HR)N2 = « -0,0162 + (0,038. 0,0434) ). 8,314. 126,2) 14,2
= -3,6350 kkal/kmo1
= -3,6350 kkal/kmol x 414,6227 kmol = -1507,1624 kkal
(HR)m = « -0,0204 + (0,022. 0,0271)).8,314. 154,6) 14,2
= -6,0606 kkal/kmol
= -6,0606 kkal/kmol x 20,2845 kmol = -122,9369 kkal
(HR)No = « -0,0227 + (0,583. 0,0092) ). 8,314.180,2) 14,2
= -6,1841 kkal/kmol
= -6,1841 kkal/kmol x 1,4692 kmol = -65,1514 kkal
(HR)N02 = « -0,0605 + (0,141. -0,0097) ). 8,314 .180,2 ) 14,2
= -37,9163 kkal/kmol
= -37,9163 kkal/kmol x 1,4315 kmol = -130,5666 kkal
B-S2
AQQendiks B
42028,2241 kkal
2019,1029 kkal
HNl = HigN2 + (HR)N2 = 43535,3865 - 1507,1624
Ha2 = Hig02 + (HR)02 = 24990,4646 - 122,9369
HNO = HigNO + (HR)No = 12721,4455 - 65,1514
HN02 = HigN02 + (HR)N02 = 58,7701 - 130,5666
= 1025,2582 kkal
-125,5292 kkal
Total panas keluar = 543803,9725 kkal
Panas mas uk + Q = panas keluar + panas hi lang
41231,3750 + Q = 543803,9725 + (0,05 * 41231,3750)
Q = 531193,8592
Kebutuhan steam :
A = 1940,75 kj / kg
m=Q A
531193,8592 m=--~-
1940,75
m = 273,7055 kg / jam
Neraca panas:
Masuk
Panas bahan
Panas disuplai
Total
Prarencana Pabrik Asaro Nitrat
kkal / jam Keluar
41231,3750 Panas bahan
531193,8592 Panas yang hiIang
572425,2342
kkal/jam
543803,9725
28621,2617
572425,2342
B-53
AppendiksB
8. Kompresor (G-121 & G-122 )
Udara masukpada suhu = 30°C
Suhu rata-rata = (30 + 25)/ 2 = 27,5 °C
Massa N2 masuk = 5790,6573 kg / jam = 206,8092 kmol/jam
Massa 02 masuk = 1759,1870 kg/jam = 54,9746 kmol/jam
Massa H20 masuk = 132,1223 kg / jam = 7,3401 kmo1/jam
Dari Kern fig. 3 :
Cp N2 = 0,23 Btu lIb OF = 0,23 kka\ I kg °C
Cp 02 = 0,21 Btu /lb OF = 0,21 kkal / kg °C
Cp H20 = 0,44 Btu I \b OF = 0,44 kka\ I kg °C
H N2 = m * Cp * ~ T = 5790,6573 * 0,23 * ( 30 - 25)= 665,2559 kkal
H 02 = m * Cp * ~T = 1759,1870 * 0,21 * (30 - 25)= 1847,1464 kkal
H H2O = m * Cp * t.T = 132,1223 * 0,44 * (30 - 25)= 2906691 kkal
Total panas masuk = 2803,0714 kkal
Udara keluar pada suhu = 306,25°C
Suhu rata-rata = (306,25 + 25 )/2 = 185,62°C
Dari Kern fig. 3 :
Cp N2 = 0,26 Btu lIb OF = 0,26 kkall kg °C
Cp 02 = 0,23 Btu / Ib OF = 0,23 kkall kg °C
Cp H20 = 0,46 Btu lIb OF = 0,46 kkall kg °C
Hig N2 = m * Cp * ~T = 5790,6573 * 0,26 * ( 306,25 - 25)= 423435,6523 kkal
Hig 02 = m * Cp * ~T = 1759,1870 * 0,23 * (306,25 - 25)= 113795,7547 kkal
Hg H2O = m * Cp * t. T = 132,1223 * 0,46 * ( 306,25 - 25 )= 17093,0706 kkal
Prarencana Pabrik Asam Nitrat
B-54
Appendiks B
Dari Smith Van Ness app.B
Tc N2 '" 126,2 K
Pc N2 '" 34 atm
(j) NH2 = 0,0,038
Tc 02 '" 154,6 K
Pc 02 '" 50,43 atm
(j) 02 = 0,022
Tr N2 306,25 + 273 4,5899 126,2
PrN2 '" 9.86 = ° 29 34 '
Tr 02 = 306,25 + 273 - 3 7467 154,6 '
Pr 02 = 9.86 = 01955 50,43 '
Dari Smith Van Ness app B:
(HR)o -'-R-r--'--N2 = - 0,0023
c
(HRy --N2 =00237
RT ' c
Prarencana Pabrik Asam Nitrat
TcH20 = 647,1 K
Pc H20 = 220,5 atm
(j) H20 = 0,345
Tr H2O = 306,25 + 273 0,8951 647,1
PrH20= 9,86 =00447 220,5 '
(HR)1 --H2O = -0 0641
RT ' c
B-55
Appendiks 8
(HR)Nz = « -0,0023 + 0,Q38. 0,0237 ). 8,314 . 126,2) / 4,2
= -0,3496 kka1Jkmol
= -0,3496 kkallkmol x 206,6092 kmol = -72,2989 kkal
(HR)02 = « -0,0118 + 0,022.0,0308 ). 8,314 . 154,6) / 4,2
= -3,4038 kkallkmol
= -3,4038 kkallkmol x 54,9746 kmo1 = -187,1245 kkal
(HR)mo = « -0,0533 + 0,345. (-0,0641) ). 8,314 . 647,1) / 4,2
= -96,6022 kkal/kmo1
= -96,6022 kkallkmol x 7,3401 kmo1 = -709,0723 kkal
HNl = HisNZ + (HR)N2 = 423435,6523 + -72,2989 423363,3534 kkal
Hoz = Hig02 + (HR)02 = 113795,7547 + -187,1245 113608,6301 kkal
Hmo = HigH20 + (HR)H2o = 17093,0706 + -96,6022 = 16383,9983 kkal
Total panas keluar = 548547,4660 kkal
Panas masuk = panas keluar + Q
2803,0714 = 548547,4660 + Q
Q = 548351,7709kkal
Neraca panas :
Masuk kkal / jam Keluar kkal / jam
Panas bahan 2803,0714 Panasbahan 548547,4660
Panas karena kompresi 548351,7709
Total 548547,4660 548547,4660
Prarencana Pabrik Asarn Nitrat
8-56
AppendiksC
APPENDIKSC SPESIFIKASI ALAT
1. FILTER UDARA (H-120)
Fungsi : untuk menghilangkan debu dalam udara masuk
Tipe : bag filter
Col
Kapasitas filter = 400 - 1800 Ib/fl?hari
Diambil kapasitas 1800 Ib/W hari
(Perry 3ed, hal 990 )
Rate udara masuk = 7681,9666 kwjam = 16935,5523 lb/jam
Flow area = rate _udara _x _24jam 16935,5523 .. 24 = 2258074 ft2 kapasitas _filter . 1800 '
Spesifikasi :
,Tipe : bag filter
Kapasitas : 1800 Ib/ft2hari
Flow area : 225,8074 ft2
2. TANKI PENAMPUNG NH3 (F-llO)
Fungsi : untuk menyimpan NH3 dalam bentuk cair selama 1 minggu
Bentuk : tanki silinder vertikal dengan tutupelliptical dished head
Kondisi operasi : T =E:PO° C
P= 11 atm (Perry r, hal 2-88)
Kebutuhan NH3 = 428,9937 kW jam = 945,7533 Ib/jam
Pada P = 1 atm :
Sv NH3 liq = 1,648.10-3 m3lkg (Perry 7ed, hal 2-214)
p NH3 = lIsv = 111,648.10-3 = 606,7961 kWm3
p H2O = 995,6470 kWm3 (Perry 7ed, hal 2-91)
1 0,995 + 0,005 1,6448.10-3 606,7961 995,647 P·/aR .. NH3
P larNID = 607,9833 kWm3 = 37,93191b/ft3
Prarencana Pabrik Asaro Nitrat
AppendiksC
Direncanakan untuk persediaan 7 hari ( 168 jam)
maka volume larutan dalam tanki:
volume = 945,7533. 168 = 41887318 tY/tanki 37,9319 '.
volume cairan = 80% volume tanki
volume tanki = (100/80).4188,7318 = 5235,9148 ft3
Direncanakan !:.... = 1,5 D
v = L (".D2
)
4
5235,9148 = 1,5 ".D3
4
D3 = 3638,1574
D = 15,3801 ft = 184,5618 in
L = 1,5 x 184,5618 = 276,8427 in
Menghitung Tebal Shell
P = 14,7 psia = 161,7+(p.~.h) = 14,7 + (37,9319.-1-.0,8.23,0702)
gc 144
= 166,6 psig
P design = 1,2 x 166,6 = 199,9 psig
Direncanakan :
- bahan konstruksi stainless steel
- bentuk head eliptical dished head
PflIfencana Pabrik Asam Nitrat
C-2
Appendiks C
pari tabel 13.1, Brownel & Young:
F allowable = 18750 Ib/in2
I> =85%
P .. ri ts = (Brownel & Young, peTS 13.1)
/.&-0,6.P
199,9. 184,5618 2
18750 .. 0,85 - .0,6.199,9
= 1 1662 = I.!. in , 8
Menghitung Tebal Head
Direncanakan :
- bahan konstruksi stainless steel SS
- bentuk head eliptical dished head
Harga k = 2 (Brownel & Young, hal 133 )
V= 1/6 (2 + ~ )
= 1/6 ( 2 + 22 ) = 1
h P .. d .. v
t =----2/.& - 0,2'p
199,9 .. 184,5618
2 .. 18750.0,85 -1,2 .. 199,9
= 1,1662 in
1 1 .
= - tn 8
Mengitung kedalaman head & panjang tanki
Dari tabel 5.11
sf= 3 in
Prarencana Pabrik Asam Nitrat
C-3
Appendiks C
tinggi head = (lD/4 ) + sf + t
= 184,5618 +3+11662 4 '
= 50,3067 in
= 4,1922 ft
tinggi head = b + sf + t = 2 + l33,1447 + 0,3658 = 135,5105 in
= 11,2925 ft
Spesifikasi :
Bahan : stainless steel
Kapasitas : 5235,9148 fe
Diameter : 15,3801 ft
Tinggi tanki total : 31,4546 ft
Tinggi tutup atas : 4,1922 ft
Tinggi tutup bawah : 14,1925 ft
Tebal shell 11. : -In 8
Tebal tutup atas 1 1 . : -In 8
Tebal tutup bawah }1. : -In 8
Jumlah : 1 tanki
3. COMPRESOR
Fungsi : menaikkan tekanan udara dari tekanan } atm ke 9,86 atm
Tipe : centrifugal compressor
Perhitungan :
Tekanan masuk : 1 atm = 2116,228 Ibf/ft2
Tekanan keluar: 9,86 atm = 20866,00811bflft2
Prarencana Pabrik Asam Nitrat
C-4
Appendiks C C-5
Pressure ratio = 9,8611 = 9,86
Digunakan kompresor multi-stage karena ratio tekanan lebih besar dari 4
(Ulrich, 1984)
(rI)q=rT p, p, dimana : q = jumlah stage
(rp.Ii = 9,86
(rp,I) = 3,14
Rasio kompresi per stage = 3,14
( )
(r-l)! r
T2=Tl ~ ~
T2=303 -'-(
3 14 )(1,395-1) /1,395
I
T2 = 418,94 K = 145,94 °C
COMPRESOR STAGE 1 (G-121)
Dimana:
k = CpJCv udara = 1,395
PI = tekanan udara masuk, IbfJft2
P2 = tekanan udara keluar , Ibflft2
rp,I = tekanan keluar tiap stage
rp,T = pressure ratio
dimana: T2 = suhu keluar stage 1
T 1 = suhu masuk stage 1
(Peters 400, pers,14-27)
qfin = kecepatan volume gas pada kondisi masuk, ft3Jmin
p pada 30°C = 0,0808 IbJft3 (Perry 600, table 3-30)
rate udara masuk = 7681,9666 kg/jam = 16935,55231bJjam
= 16935,5523 2095984196 feram = 34933070 ft3Jmin qfin 0 0808 ' J , ,
h = 3,03,10-5.1,395.2116228 .. 34933070,(314(0,39511,395) -1)
P 1,395 -1 ' , . '
= 302,6942
Efisiensi motor = 70% (Peters 400, hal 524 )
Prarencana Pabrik Asaro Nitrat
AppendiksC
Hp motor = 302,6942 432,4203 bp 0,7
Spesifikasi :
Tipe : centrifugal compressor
Pressure ratio = 3,14
Daya motor = 432,4203 hp
Bahan: stainless steel
COMPRESOR STAGE 2 (G-122)
Tekanan udara masuk stage 2 = 3,14 atm = 6644,9559Ibflft2
( )
(r-I)/ r
T2=Tl P2 ;:;
. (9 86)(1.395-1)/1.395 T2 = 418 94 -'-
, 314 ,
T2 = 579,25 K = 306,25 °c p pacta 306,25 °c = 0,2537 Ib/ft3
dimana : T2 = suhu keluar stage 2
Tl = suhu masuk stage 2
rate udara masuk = 7681,9666kgljam = 16935,5523 Ib/jam
qfm = 16935,5523 323815,5315 fe/jam = 5396,9255 ft3/min 0,0523
h = 3,03.10-5.1,395.66449559 .. 53969255.(314(0.395/1.395) -1) p 1395 -1 ' , , ,
C-6
= 1468,3968
Efisiensi motor = 70% (Peters 4ed, hal 524 )
Hp motor = (1468,3968 / 0,7) = 2097,71 hp
Spesifikasi :
Tipe : centrifugal compressor
Pressure ratio: 3,14
Daya motor: 2097,71 hp
Bahan: stainless steel
Prarencana Pabrik Asam Nitrat
Appendiks C
4 .HEAT EXCHANGER (E-212)
T2 i 392"F
.1 HE udara tI = 860f
f I----+~ t2 = 392"F
Gas 1652 Op
Fungsi : untuk mendinginkan udara keluar dari oksidator 1
Tipe : shell and tube
Perhitungan :
Neraca Panas
m gas = 8110,9603 kg/jam = 17904,96313lb/jam
M udara = 36721,4125 kg/jam = 81062,7208 Ib/jam
Q = 1560660,0298 kkaVjam = 613095,353 btu/jam
LTMD = (392 - 86) - (1652 - 356) = 685 86"F In (392 - 86) ,
(1652-356)
R = 1652-392 467 356- 86 '
S = 356-86 0,1741 1652 - 86
Ft = 0,87 (Kern, fig. 18)
nt = 0,87.68,6 = 596,7 OF
Tc = (1652 + 392)/2 = 1022°F
tc = (86 + 356)/2 = 221°F
Trial Uo= 20
A = Q = 6193095,353 518,95 Ud.AT 20.569,7
Prarencana Pabrik Asam Nitrat
C-7
Al1l1endiks C
Ditetapkan:
OD tube = 1 in, 10 BWG
ill tube = 0,732 in
L = 12 ft
a" = 0 2618 ft2 ,
C-8
( Kern, table 10)
Jumlah tube = ~= 518,95 165,1851 a" .. L 0,2618 .. 12
Dari tabel 9 Kern, untuk square pitch
PI = 1 ~in 4
Nt standar = 166 buah
Passes = 2
ill shell = 21 ~ in 4
. 1651851 Uo terkoreksl = ' .20 = 19,9018
166
Shell, gas
1 1 C' =PI-OD= 1-- I =-
4 4
3 1 B= -.21- =159375
4 4 '
111 as = ID .. c'B _ 21 4"14.15,9375
I 44.Pr 144. I.!. 4
= 0 4704 ft2 ,
Gs = W = 17904,9634 as 0,4704
= 38065,0842 Ib/jam ft
Pada Tc = 1022"F
Prarencana Pabrik Asam Nitrat
Tube, udara
a't = 0,421 (tabellO)
Nt .. a't at=--
144 .. n 166xO,421 0,2427 W
144x2
Gt = ~ = 81062,7208 at 0,2427
= 334059,2335 lb/jam ft
Pada tc = 221 "F
~ = 0,0225 . 2,42 = 0,0545 Ib/jam ft
(fig. 14)
c = 0,25 (fig. 2 )
Appendiks C C-9
Il = 0,034.2,42 = 0,0823 lb/jam ft k = 0,0157 (tab. 4 )
(fig. 15) D = 0,732/12 = 0,061 ft (tab. 10)
De = 0,99/12 = 0,0825 (fig. 28)
c = 0,2878 (fig. 3 )
k= 0,0369 (tab. 5)
Res = D.Gt = 0,0825.38065,0842 P 0,0823
= 38157,5874
jH = 105 (fig. 28)
1 1
(C.J.I}3 =(0,2878.0,0823)3 = ° 8626 k 0,0369 '
1
~ =jH(~SXC:y = 105 0,036908626= 405108
00825 ' , ,
ho
tw=tc+ h" t/Js h (Tc-tc) 10 0 -+-¢X t/Js
Ret = D.Gt = 0,061.334059,2835 P 0,0545
= 373901,1604
L 12 - = -- = 1967213 D 0,061 '
jH=750 (fig. 24)
1 1
(C.p)3 =(0,25.0,0545}3 = 0 9538 k 00157 '," ,
1
hi _ "H( k XC.p )3 --j - -
¢X D k
= 750(°,0157)0 9538= 184 1147 0061' , ,
hio = hi.lD = 1841147. 0,732 ¢X ¢X OD ' 1
= 134,7720
= 221+ 40,5108 (1022 - 221) 134,7720 + 40,5108
= 406, 124'1'F
Pada tw = 406, 1241'F pada tw = 406, 124'1'F
Ilw = 0,0295.x 2,42 = 0,0713 (fig.15) Ilw = 0,0124.x 2,42 = 0,03 (fig. 14)
Prarencana Pabrik Asaro Nitrat
Appendiks C C-IO
tIE = L = 0,0823 = 1,0203 ( )
0.14 ( )0.14
f.JW 0,0713 ¢t = L = 0,545 = 1,5007
( )
0.14 ( )0.14
f.JW 0,03
ho = 40,5108 x 1,0203 = 41,3332 hio = 134,7720 x 1 ,5007 = 146,5106
U - hio .. ho
c-hio+ho
41,3332 .. 146,51 06 32,2382 41,3332 + 146,5106
Rd = Uc - Uv = 32,2382 -19,9018 0,019 Uc . .uv 32,2382.19,9018
(memenuhi > 0,003)
Perhitungan pressure drop
Shell, gas
Nres = 38157,5874
f=0,0017 (fig. 29)
N+l = L.12= 12 .12=90353 B 15,9375 '
BM campuran = 26,9112 kglkmol
P.BM 9,37.26,9112 P gas = = -c-_-'--_
R.T 0,0821.798
= 3,8488 kg/m3 = 0,2403 Ib/ft3
s = 0,2403 0 0038 625 ' ,
IDs=21.!. in=I,7708ft 4
AD _ f·Gs 2.1Ds.(N + 1) Ll1S- 10
5,22.10 .De.s.t/xs
= 0,0017(38157,5874)2.1,7708.9,0353 5,22.1010.0,0825.0,0038.1,0203
Prarencana Pabrik Asam Nitrat
Tube, udara
Nret = 373901,1604
f= 0,000105
pudara = 0,05351b/ft3
(fig. 26)
(Geankoplis, Tabel A-3.3)
s = 0,535/62,5 = 0,0086
A D _ f.Gt 2.L.n Ll1 t - 10
5,22.10 D.s.¢t
= 0,000105(373901,1604)2.12.2 5,22.1010.0,061.0,0086.1,5007
=0,8573 psi
v -=00013 2g' '
~Pr= 4n~ S 2g'
(fig. 27)
AppendiksC C-ll
- 4.6 00013= 06279 i 00086 ' , ps ,
= 2,3732 psi
(memenuhi < 10 psi)
M., = 0,8573 + 0,6279 = 1,4852 psi
(memenuhi < 2 psi)
Spesifikasi:
Tipe : shell & tube
Shell: ID = 21 ~ in; baffle space = 15,9375 in; passes = 1 4
Tube: OD = 1 in; 10 BWG; L = 12 ft; passes = 2; Pr= 1 ~in (square pitch) 4
Jumlah tube: 166
Ud= 19,9018
Uc = 32,2382
Rd=0,019
. M> shell = 2,3732 psi
~P tube = 1,4852 psi
5. TANK! PENAMPUNG RN03 (F-31O)
Fungsi : untuk menyimpan RN03 selama 1 hari
Bentuk : tanki silinder horisontal bertekanan 1 atm dengan tutup elliptical
dished head
Kondisi operasi : T = 30° C
P = 1 atm
Rate = 1903,8903 kgl jam = 4197,2890 Ib/jam
Pada 1 atm dan 30°C:
SgRN03 = 1,504. m1Jkg
p RN03 = (1,504/1).62,43 = 93,89471b/ft3
p H2O = 995,6470 kglm3 = 62,1582 Ib/ft3
1
P·laR.HN03
0,6 + 0,4 0,0128 93,8947 62,1582
Prarencana Pabrik Asam Nitrat
(perry 7ed, haI2-214)
(Perry 7ed, hal 2-91)
Appendiks C
P larHN03 60% = 110,0128 = 77,97071b/ft3
Direncanakan:
untuk menampung hasil produksi selama 1 hari
- memakai 1 tanki penyimpan
maka volume larutan dalam tanki:
volume = 4197,2890.24 = 1291 9589 ft3 77,9707 '
volume cairan = 80% volume tanki
volume tanki = (100/80).1291,9589 = 1614,9486 ft3
. k L 1 Duencana an - = ,5 D
v = L (7(.D2
)
4
1614,9486 = 1,57(.D3
4
= e: 7( )D3
D3 = 1371 71 ,
D = 11,1105 ft = 133,3257 in
L = 1,5 x 133,3257 = 199,9885 in
Menghitung T ebal Shell
P = 1 atm = 14,7 psia = 14,7 + (77,9707.(1/144).0,8.16,6657)
= 21,9191 psig
P design = 1,2 x 21,9191 = 26,3029 psig
Direncanakan :
- bahan konstruksi stainless steel SS
- bentuk head eliptical dished head
Prarencana Pabrik Asarn Nitrat
C-12
AppendiksC C-13
Dari tabel 13.1, Brownel & Young:
F allowable = 18750 Ib/in2
E =85%
ts = P .. ri (Brownel & Young, pers 13.1) f.c-O,6.P
26,3029. 133,3257 2
18750 .. 0,85 - .0,6.26,3029
= ° 11 Olin = .!. in , 8
Menghitung Tebal Head
Direncanakan :
- bahan konstruksi stainless steel SS
- bentuk head eliptical dished head
Harga k = 2 (Brownel & Young, hal 133 )
V= 1/6 (2 + ~ )
= 116 ( 2 + i ) = 1
h P .. d .. v
t =----2f.c-0,2'p
26,3029 .. 124,6473
2 .. 18750.0,85 - 0,2 .. 26,3029
= ° 1101 in = .!.. in , 8
Menghitung tinggi head
tinggi head = t + sf + (ID/4)
dari tabel 5.11
sf= 3 in
tinggi head = 0,11 + 3 + 133,:257
= 36,4414 in·
= 3,0368 ft
Prarencana Pabrik Asam Nitrat
Appendiks C
Menghitung tebal tutup bawah yang berbentuk flat
t = c. D. (P/f)112
t = 133,3257.(26,3029/18750)112
= 4,9936 in = 5 in
Spesifikasi :
Bahan : stainless steel
Kapasitas : 1614,9486 fe Diameter : 11,1105 ft
Tinggi tanki total : 24,7025 ft
Tinggi tutup atas : 3,0368 ft
Tebalshell : 1/8 in
Tebal tutup atas : 1/8 in
Tebal tutup bawah : 5 in
lumlah : I tanki
6. OKSIDATOR 2 (R-230)
Fungsi : untuk membentuk N02 dari NO dan O2 dalam gas
Tipe : reaktor plug flow
Reaksi : NO + Y:z 02 ------- N02
Konversi reaksi = 95 %
Suhu gas masuk = 200°C
Lo k = 652,1 -1 0366 = 652,1 1,0366=0,3420 g T' 200+273
k=21981 S·1 ,
FAD = 526,3691 lbmol I jam
x. P 0,1214.9,37 3 CAD = -- = = 0,01831bmol I ft
R. T 0,729. 852
Prarencana Pabrik Asam Nitrat
C-14
AppendiksC
= 526,3691 ((1 + 1)ln 1 -1. 0.95) 3600.2,1981.0,00183 1-0,95'
= 183,2509 fe L= 1,5 D
V=( 1,5/4).3,14. D3
183,2509 = (1,5/4 ). 3,14. D3
D = 5,3789 ft = 64,547 in
L = 1,5 x 64,547 = 96,821 in
Menghitung tebal shell
P = 137,739 psia = 152,439 psig
P design = 1,2 x 152,439 = 182,93 psig
Direncanakan :
- bahan konstruksi stainless steel SS
Dari tabel 13.1, Brownel & Young :
F allowable = 18750 Ib/in2
E =85%
ts = P .. ri (Brownel & Young, pers 13.1) j.&-0,6.P
182,93. 96,821 2
18750 .. 0,85 - .0,6.182,93
. 5. =05595 m= - m , 8
Menghitung Tebal Head
Direncanakan :
- bahan konstruksi stainless steel SS
- bentuk head eliptical dished head
Harga k = 2 (Brownel & Young, hal 133 )
Prarencana Pabrik Asam Nitrat
C-15
Appendiks C
V= 116 (2 + ~ )
= 116 ( 2 + 22 ) = 1
h P .. d .. v
t =----2j.c-0,2.P
182,93 .. 96,821
2 .. 18750.0,85 - 0,2 .. 182,93
O .5 .
= 5563 m= - m , 8
Menghitung tinggi head
tinggi head = t + sf + (ID/4)
dari tabel 5.11
·sf= 3 in
tinggi head = 0,5563 + 3 + 96~21
= 27,7612 in
= 2,3134 ft
G= W = 14431,7960 as 0,453. 0,25.3,14. (8,068)2
= 623,4774 lb/jam ft
Pada Ie = 392"F
Il = 0,0404.2,42 = 0,0978Ib/jam ft (fig. 15)
e = 0,2698 (fig. 3 )
k = 0,0289 (tab. 5)
D.Gt 8,068. 623,4774 Res =--= -----
J.l 0,0978
= 51436,3543
Prarencana Pabrik Asam Nitrat
C-J6
AppendiksC
I
; = Nre( ~ X c; J = 51436 3543 0,028909690= 1785360
, 8068' , ,
asumsi $ =1
hio = hi. (ID/OD)
= 178,5360. (8,068/(8,068 + 0,0466)
= 177,5102
hio ho 177,5102. 178,5360 Uc = .. = 89,0108
hio + ho 177,5102 + 178,5360
Rd = 0,01 ( Kern, tabeI 12 )
III - = -+ Rd = + 0,01 = 0,02123 Ud Uc 89,0108
Ud = 47,093
A = Q = 812433,5238 = 345 0339 ft2 Ud.flT 47,093. SO '
Spesifikasi:
Tipe : reaktor plug flow
Bahan : stainless steel
Kapasitas : 183,2509 ft3
Diameter : 8,068 ft
Tinggi tanki total : 16,7288 ft
Tinggi tutup atas : 2,3134 ft
Tinggi tutup bawah : 2,3134 ft
Tebaishell : 5/8 in
Tebal tutup atas : 5/8 in
Tebal tutup bawah : 5/8 in
Jumlah : 1 tanki
Prarencana Pabrik Asam Nitrat
C-17
Al1l1endiks C
7. CONDENSER (E-232)
Air pendingin tl = 82,4°F ~
condensor t2 = 118,4OP
gas T1 3920P
Fungsi : untuk mendinginkan gas dari suhu 3920P ke 950P
Tipe : shell and tube
Perhitungan :
Neraca Panas
m gas = 14431,7980 kg/jam = 31816,1332 Ib/jam
Mair =59171,1061 kg/jam = 130447,7648 Ib/jam
Q = 1183422,1224 kaI/jam = 4696119,532 btu/jam
LTMD (95-82,4)-(392-118,4) = 8483 of In (95-82,4) ,
(392-118,4)
R = 392 - 95 8,25 118,4-82,4
S = 118,4-82,4 0,0116 392-82,4
Fr = 0,98 (Kern, fig. 18)
.M = 0,98. 84,83 = 83,132 OP
Tc = (392+95)/2 = 243,5 OP
tc = (118,4+82,4)/2 = 100,4 OP
Trial Do= 30
A = Q = 4696119,532 - 1845,3366 Ud .!1T 30. 84,83
Ditetapkan:
OD tube = 1 in, 10 BWG
ill lube = 0,732 in
Prarencana Pabrik Asarn Nitrat
(Kern, table 10)
C-lS
Appendiks C C-I9
L = 12 ft
a" = ° 2618 ft2 ,
J lah t b - A _ 1845,3366 urn u e - --- ---'---
a" .. L 0,2618 .. 12 587,3875
Dari tabel 9 Kern, untuk square pitch
1 . Pr= I-m
4
Nt standar = 596 buah
Passes = 1
1D shell = 37 in
. 5873875 Do terkoreksl = ' 30 = 29,5665
596
Shell, gas
C' =Pr-OD= 1.!..-1 =.!.. 4 4
3 B= -.37=27,75
4
!D .. c'B a.=
144.Pr
37. ~. 27,75
144. I.!.. 4
= 1 4260 ft2 ,
Gs= W = 31816,1332 as 1,4268
= 22298,9439 Ib/jarn ft
Pada Tc = 243,5°F
~ = 0,034. 2,42 = 0,0823 Ib/jarn ft
(fig. 15)
Prarencana Pabrik Asaro Nitrat
Tube, air
a't = 0,421 (tabell0)
Nt .. a't 596xO,421 at= - ---'--
144 .. n 144xl
= 1,7425 W
Gt = ~= 130447,4648 at 1,7425
= 74862,24571b/jam ft
Pada tc = 100,4 OP
~ = 0,0225 . 2,42 = 0,0545 lb/jarn ft
(fig. 14)
c = 0,25
k = 0,0157
D ~ 0,732/12 = 0,061 ft
(fig. 2 )
(tab. 4 )
(tab. 10)
~A~pp~en~d~jk~sC~ __________________________ ~C-20
De = 0,99/12 = 0,0825 (fig. 28)
c=0,2878 (fig. 3 )
k = 0,0369 (tab. 5)
D.Gt 0,0825 .22311,4539 Res =--= --------
P 0,0823
= 22365,6737
jH = 150 (fig. 28)
I I
(C.p )3 =(0,2878.0,0823}3 = 08626 k 0,0369 '
I
: =jH(~sXc:J = 150 0,036908626= 578726
0,0825 ' ,
ho
tw=tc+ h. t/JS h (Tc-tc) /0 0 . -+-¢X t/JS
D.Gt 0,061. 74862,2467 Ret = --= ------
P 0,0545
= 83790,7715
L 12 - = -- = 1967213 D 0,061 '
jH =400 (fig. 24)
I I
(C.p )3 =(0,25.0,0545)3 = 0 9538 k 0,0157 '
I
hi _ ·H( k XC.J.1.)3 --J - -¢X D k
= 400(0,0157}0 9538= 98 1945 0061' , ,
= 71,8784
= 1004+ 57,8726 (2435-1004) , 71,8784 + 57,8726 ' ,
= 164,23"F
Pada tw = 189 ,54°F pada tw = 189,54 "F
Ilw = 0,0264.x 2,42 = 0,064 (fig. IS) Ilw = 0,0196.x 2,42 = 0,0474
(fig. 14)
Prarencana Pabrik Asam Nitrat
Appendiks C C-21
fjx; = (L)0,14 = (0,034)°'14 = 0,9153 JlW 0,064
f/X = (L)0,14 = (0,0545)°,14 JlW 0,0474
= 1,0196
ho = 57,8726 x 0,9153 = 52,9708 hio = 71,8784 x 1,0196 = 73,2872
Dc = hio .. ho = 52,9708 .. 73,2872 30,7472 hio + ho 52,9708 + 73,2872
Rd= Uc-Un = 30,7472-29,5665 0,0031 Uc . .u n 30,7472 .29,5665
(memenuhi > 0,003)
Perhitungan pressure drop
Shell, gas Tube, air
Nres = 22365,6737
f= 0,0016
Nret = 83790,7715
(fig. 29) f= 0,00011 (fig. 26)
L 12 N+l = -.l2= --.l2=51825
B 27,75 '
BM campuran = 28,4158 kglkmol
P.BM 9,37.28,4158 pgas= -
R.T 0,0821.516,5
= 6,2789 kglm3 = 0,39171b/ft3
s = 0,3917 00063 625 ' ,
IDs = 37 in = 3,0833 ft
AD _ j.Gs2.IDs.(N + 1) urS - 10
5,22.10 .De.s.fjx;
= 0,0016(22365,6737)2.3,0833.5,1892
5,22.1010.0,0825.0,0063.0,9153
Prarencana Pabrik Asam Nitrat
pair = 62,5 Ib/ft3
(GeankopIis, Tabel A-3.3)
s = 62,5/62,5 = 1
A D _ f.Gt 2 .L.n ill t - 10
5,22.10 .D.s.f/X
= 0,000155(83790,7715)2.12.1
5,22.1010.0,061.1.1,196
=0,0034 psi
v -=0001 2g' '
~Pr= 4n~ s 2g'
4.1 =-0004 = 0016 psi l' ,
(fig. 27)
Appendiks C C-22
= 0,5157 psi M} = 0,0021+0,016 = 0,0194 psi
(memenuhi < 10 psi) (memenuhi < 2 psi)
Spesifikasi:
Tipe : shell & tube
Shell: ID = 37 in; baffle space = 27,75 in; passes = 1
Tube: OD = 1 in; 10 BWG; L = 12 ft; passes = 1; Pr = 1 ! in (square pitch).
Jumlah tube: 596
Ud= 29,5665
Uc = 30,7472
Rd = 0,0031
LiP shell = 0,5157 psi
LiP tube = 0,0194 psi
8. BAG FILTER (H-220)
Fungsi : untuk mengambil platinum yang terikut pada gas keluar dari
oksidator 1
Perhitungan :
Kapasitas filter = 400 - 1800 Ib/ft2hari
Diambil kapasitas 1800 lb/~hari
Rate gas masuk = 8110,9603 kg/jam = 17881,3058Ib/jam
Flow area = flow _area _x _24jam - 17881,3058 .. 24 238,4474 ft2 kapasitas _filter 1800
Spesifikasi :
Type : bag filter
Kapasitas: 1800 lb/~hari
Flow area : 238,4474 ft2
Jumlah: 1
Prarencana Pabrik Asam Nitrat
Appendiks C
9. BLOWER 1 (G-231)
Fungsi : untuk mengalirkan gas dari oksidator 1 menuju bag filter
Tipe : centrifugal
Kondisi operasi : T = 400°C
P = 1 atm
BM gas = 27,17 g/mol
p gas = P. BM 1 R. T
= 1.27,17/0,0821. 673 = 0,4917 kglm3
rate gas = 8110,9603 kg/jam
rate volumetrik = 8110,9603 10,4971 = 16316,5566 m3/jam
= 9603,1094 fe Imenit
C-23
h - 144 .. qfm.(~ - ~) (Perry 5ed, hal 6-20) p- 33000
= 144 .. 9603,1094.(9,5 - 9,37)
33000
= 5,4476 hp
effisiensi = 75%
power = 5,4476 10,75 = 7,2634 hp
Spesifikasi :
Tipe : centrifugal
Rate: 9603,1094 fi?/menit
Power: 7,2634 hp
Bahan : stainless steel
Prarencana Pabrik Asarn Nitrat
~A~pp~eillndillik~s~C~ ________________________________________ ~t-24
to. BLOWER 2 (G-241)
Fungsi : untuk mengalirkan gas dari kondensor menuju menara absorber
Tipe : centrifugal
Kondisi operasi : T = 35°C
P = 1 atm
BM gas = 29,1794 g/mol
p gas = P. BM I R. T
= 1.29,1794 I 0,0821. 308 = 1,1539 kg/m3
rate gas = 14431,7960 kg/jam
rate volumetrik = 14431,7960 11,1539 = 12506,9726 m3/jam
= 7360,9789 ft3/menit
h - 144 .. qfin.(~ -~) p- 33000
= 144 .. 7360,9789.(9,5-9,37)
33000
=4,1757hp
effisiensi = 75%
power = 4,1757 /0,75 = 5,5676 hp
Spesifikasi :
Tipe : centrifugal
Rate: 7360,9786 ft3tmenit
Power: 5,5676 hp
Bahan : stainless steel
11. FURNACE (Q-211)
(Perry 5ed, hal 6-20)
Fungsi : untuk memanaskan gas yang akan masuk ke oksidator 1
Kondisi operasi :
Suhu gas masuk = 30°C
Suhu udara masuk = 30°C
Prarencana Pabrik Asam Nittat
Al'l'endiks C
Suhu fuel oil masuk = 30°C
Suhu gas keluar = 850°C
Suhu flue gas keluar = 1200°C
C-2S
Panas yang diterima furnaCe = 1413835,5248 kkalljam = 5610458,429 btu/jam
Bahan bakar masuk = 321,3508 kg/jam
Direncanakan dapur berukuran : lOx 15 x 5 ft
Luas permukaan dinding total = 2(5. 15) + 2(5. 10) + 2(10. 15) = 550 ft2
Kehilangan panas melalui dinding 20%
Panas yang hilang = 0,2.5610458,429 = 1122091,686 btu/jam
Tl= 86"F
Suhu rata-rata = (1562 + 86 )/2 = 824°F
q = 1122091 /550 = 20401667 btu/jam W
hc = CI. k. (a. . .1t)1I3
a. udara = 0,0353.106 (ft3 "Frl
k udara = 0,0308btu/jam ft "F
CI = 0,13
d = 1/3
1. Insulating fire brick
II. Fire clay brick
hc = 0,13.0,0308. (0,0353.106. 1476)113 = 1,4955 btu/jam W"F
hr = T.Fe.Fr.(ts4
- tr4
)
ts-tr ts = 1562°F =2022"R
tr = 86"F = 456"R
t = konstanta Boltzman = 0,173.10-8
Fr= 1
Fe= 0,75
hr = 0,173.10-8.0,75.1.(2022
4 - 546
4) = 20,0391 btu/jam rr"F
2022-546
ho = hc + hr = 1,4955 + 20,0391 = 21,5346 btu/jam W"F
Prarencana Pabrik Asaro Nitrat
Appendiks C
Dari table 2, Kern :
k insulating fire brick = 0,309 btu/jam ft2°F
k fire clay brick = 0,9125 btu/jam ft2°F
1562-86 2040,1667 = --------
x x 1 ~-+ +---0,0309 0,9125 21,5346
x = 0,1563 ft
Digunakan tube dengan ukuran 2"sch 40, dengan panjang 12 ft
Dari table 11, Kern :
ID = 2,067" = 0,1723 ft
OD = 2,38" = 0,1983 ft
a" = 0 622 ft2 ,
Rate gas masuk = 17881,3058Ib/jam
Dari Kern:
Cp = 0,3011 btullboF
).1 = 0,0318 . 2,42 = 0,0769 lb/jam ft
k = 0,0338 btu/jam ft2(Dp/ft)
(figure 3 )
(figure 15)
(table 4)
G = rate = 17881,3058 767289,0814Ib/jam W 1£ D2 1£ 0 17232
4 4 '
h~D = 0,0115{ D~G r9
(c; rs (Kern, pers. 3-42)
hi.0,1723 = 001l5.(0,1723.17881,3058}O.9(0,3011.0,0769}o.S 0,0338' 0,0769 0,0338
hi = 36,4448 btu/jam UZOP hio = hi .(ID/OD) = 36,4448.(2,067 12,38) = 31,6518 btu/jam ft2Dp
Prarencana Pabrik Asam Nitrat
C-Z6
Appendiks C
U hio.ho
c=---hio+ho
31,6518 .. 36,4448 16,9398 31,6518 + 36,4448
Dari table 12, Kern :
Rd gas = 0,002
Rd fuel oil = 0,005
Rd gabungan = 0,007
1 1 - == - + Rd = (11 16,9398) + 0,007 = 0,066 Ud Uc
Ud= 15,144
Q=Ud.A.dT
5610458,4290 = 15,144. A. (1562-86)
A = 250,9987 ft2
A = Nt. a".L
250,9987 = Nt. 0,622. 12
Nt = 33,6279 = 34 buah tube
Spesifikasi :
Ukuran furnace : 5 x 10 x 15ft
Tebal dinding : 0,1563 ft
Jumlah tube : 34 buah
ID tube : 2,067 in
ODtube : 2,38 in
Panjang tube : 12 ft
Jumlah alat : 1
12. OKSIDATOR 1 (R-21O)
Fungsi : untuk mereaksikan NH3 menjadi NO dan H2O dengan katalis
platinum- rhodium berbentukkawat kasa
Kondisi Operasi : suhu : 850°C = 1562°F
Prarencana Pabrik Asam Nitrat
C-27
Appendiks C
Tekanan : 9,37 atm = 137,739 psi
Komposisi gas masuk :
Gas kg/jam kmol/jam fraksi mol
02 1759,1870 54,9746 0,1868
N2 5790,6573 206,8092 0,7026
H2O 134,2672 7,4593 0,0253
NH3 426,8487 25,1087 0,0853
'Reaksi :NH3(g) + 5/4 02 ------ NO(g) + 3/2 H20(g)
Konversi reaksi : 99,9%
x = I - exp (-k.g.a.e)
0,999 = 1 - exp (-kg.a.e)
0,001 = exp (-kg.a.e)
In 0,001 = - k g. a. e
kg.a.e = 6,9
k e 4.n .g.a. =----0-7
Re'
(carberry, sec. 10.7)
(carberry, pers.1O-128)
(Carberry, hal 586)
dimana n : jumlah lapisan kawat platinum
Re: Reynold number ( 10 - 104)
Diambil harga Re = 10
69= 4.n , 10°,7
n = 8,6 ""' 9 buah
Dari figure 15, Kern:
f.L NH3 = 0,04. 2,42 = 0,0968 Ib/jam ft
f.L 02 = 0,051. 2,42 = 0,1234Ib/jam ft
f.L H20 = 0,046. 2,42 = 0,1111 Ib/jam ft
f.L N2 = 0,047.2,42 = 0,1137Ib/jam ft
C-Z8
f.L gas campuran = (0,0968 113.0,0871)+(0,1234113.0,1908)+(0,1111 113.0,0043)
+(0,1137113.0,7178)
= 0,1141 Ib/jam ft
Prarencana Pabrik Asam Nitrat
Dari table 3-30, Perry 6ed :
p NH3 = 0,0482 Ib/ft2
P 02 = 0,0892 Ib/ft2
P N2 = 0,0782 Ib/ft2
P H2O = 0,911blttl
I ::: 0,0871 + 0,1908 + 0,0043 + 0,7178 13,1298 Pcampuran 0,0482 0,0892 0,91 0,0782
p campuran = 0,0762 Ib/ft2 ( pada STP )
cam uran ada 137739 si dan 15620 F = 0,0762.(32 + 460). 137,739 p P p , P 14,7 (1562+460)
v = f.J = 0,1141 1,497 ft3/jam ft P 0,0762
Re=dw.uIV
10 = 2,5.10-4. U/l,497
U = 59878 ftljam = 997,9667 ftlmenit
=0,17371b/ft2
(Carberry, hal 586)
Rate total gas masuk = 294,3518 kmol/jam = 1O,8154Ibmol/menit
Volume Ilbmol pada 137,739 psi dan 1562"F = Vo. (PolP). (TlTo)
= 359. (14,7/137,739). (1562+460/32+460) = 667,4602 ft311bmol
Rate gas masuk (Q) = 10,8154. 667,4602 = 7218,8194 ft3/menit
= 433129,1654 ft3/jam
S = Q/u = 7218,8194 1997,9667 = 7,2335 ttl
S = 0,25 1t D2
7,2335 = 0,25.3,14. D2
D = 3,0356 ft
Prarencana Pabrik Asam Nitrat
Appendiks C
Waktu kontak dalam lapisan kawat kasa
e=dw. 1>. nlV
dimana 1>: void fraction rata-rata, diambil 0,5
e = 2,5.10-4.0,5.9/1,497 = 7,515.10-4 jam-I= 2,7054 def I
Menghitung tebal shell
P = 137,739 psi a = 152,439 psig
P design = 1,2 . 152,439 = 182,9268 psig
Direncanakan :
Bahan konstruksi stainless steel SS
Tabel 13.1, Brownell & Young diperoleh :
fallowable = 18750 Ib/in2
I> =85%
C-30
P .. ri ts=---
f,8-0,6.P (Brownel & Young, pers 13.1)
182,9268. 32,2972 2
18750 .. 0,85 - .0,6.182,9268
=01866 =! in , 4
Menghitung tebal head
Direncanakan :
- menggunakan bahan stainless steel SS
berbentuk elliptical dished head
Harga k = 2 ( Brownell hal 133 )
V= 116 (2 + ~ )
= 1/6 ( 2 + 22 ) = 1
Prarencana Pabrik Asam Nitrat
AppendiksC
h P .. d .. v
t =----2f·s-0,2'p
182,9268 .. 32,2972
2 .. 18750.0,85 - 0,2 .. 182,9268
= 01856 = ~ in , 4
Menghitung tinggi head
dari table 5.11 Brownell & Young,
sf= 3 in
tinggi head = t + sf + (ID/4)
= 3 + 0,1856 + (32,2972/4)
= 11,2599 in = 0,9383 ft
Menghitung tinggi shell
Jarak antar kawat = 1 in
Jarak antar kawat dari atas hingga bawah = (9-1). 1 = 8 in = 0,6667 ft
Tinggi ruang kosong diaffibil (atas + bawah) = 1,5 ft + 1,5 ft = 3 ft
Tinggi shell = 3+ 0,6667 = 3,6667 ft
Menghitung luas perpindahan panas
Pada Tc = 392"F
J.1 = 0,0404.2,42 = 0,0978 Ib/jam ft (fig. 15)
c = 0,2698
k =0,0289
D.Gt 2,6914. 17881,3058 Res =--= ------
Jl 0,0978
= 492083,2962
J
~ = Nre(~X c:J
(fig. 3 )
(tab. 5)
= 4920832962 0,028909690= 51201487 , 26914' , ,
Prarencana Pabrik Asam Nitrat
C-31
Al1l1endiks C C-32
asumsi. =1
hio steam = 1500 (Kern, hal. 719 )
U - hio .. ho 5120,1487.1500
c - = 1160,1285 hio + ho 5120,1487 + 1500
Rd = 0,01 (Kern, tabel12 )
_1_ = _1 + Rd = 1 + 0 01 = 0 01086 Ud Uc 1160,1285' ,
Ud= 92,0643
A = Q = 5196393,583 = 1128 8618 W Ud.!l.T 92,0643. 50 '
Spesifikasi :
Bahan : stainless steel
Kapasitas : 340490,64 fe/jam
Diameter : 2,6914 ft
Tinggi tanki total : 5,5433 ft
Tinggi tutup atas : 0,9383 ft
Tinggi tutup bawah : 0,9383 ft
Tebal shell : 114 in
Tebal tutup atas : 114 in
Tebal tutup bawah : 114 in
Jumlah : 1 tanki
Prarencana Pabrik Asam Nitrat
AppendiksC
13. POMPA 3 (L-311)
--..,1---1 L
EL-. Fungsi : mengalirkan HN03 menuju tanki penampung
Rate = 1903,8903 kg! jam = 4175,1980 lh/jam
Pada 1 atm dan 30°C:
C-33
SgHN03 = 1,504. m3/kg (Perry 7ed, hal 2-214)
p HN03 = (1,504/1).62,43 = 93,8947 lb/ft?
p H2O = 995,6470 kg!m3 = 62,1582 Ib/ft3 (Perry 7ed, hal 2-91)
1
P·laR . .HN03
0,6 + 0,4 00128 93,8947 62,1582 '
PlarHN0360%= 1/0,0128 =77,9707Ib/ft3
volume = 4175,1980.= 53,5483 ft3/jam = 0,0149 ft?ls = 6,7037 gpm 77,9707
/-l HN03 = 0,00138Ib/ft. s
Di opt = 3,9 . qrO.45
• pO•13 . (Peters & Timmerhaus, 4ed, p. 496)
= 3,9.0,0149°.45 . 77,970~·13 = 1,0350 in
Dipilih steel pipe (IPS) berukuran 1 in sch 40 :
ill = 1,049 in = 0,0874 ft .
OD = 1,32 in
A = 0,864 in2 = 0,006 ft2 (Peters & Timmerhaus, 4ed, tabel 13, p. 888)
. 00149 Kecepatan hnear =' - 2,4833 fils
0,006
p. di . v 77,9707Ib 1 ft3 ·0,0874 ft· 2,4833 ft 1 S NRe = 12262,8938
J.I 0,00138Ibmlft·s
Prarencana Pabrik Asam Nitrat
AppendiksC C-34
1 2 2 g P2-P., ---·(V2 -VI)+ -·(Z2-ZI)+ + DF+Ws=O 2·a·ge ge P
(pers 2.7-28 Geankoplis 3ed, p 275)
Dimana LF merupakan total fraksionallosses, meliputi :
1. Losses karena kontraksi , he
2. Losses karena friksi pada pipa lurus, Ft
3. Losses karena friksi pada elbow dan valve, Hf
4. Losses karena ekspansi pada bak penampung
5. Losses karena pressure drop.
Perhitungan LF :
1. Losses karena kontraksi , he
A Kc = 0,55 x (1 __ 2 )
Al
Dimana: Al = luas penampang tangki
A2 = luas penampang pipa
Karena AI»>A2 maka (A2/AI) diabaikan
Kc = 0,55 x (1-0) = 0,55
he = Ke. v2
0,55. 2,.48332
- 0,0527 ft.lbf7lbm 2·a·gc 2·1·32,174
2. Losses karena friksi pada pipa lurus, Ft
Digunakan pipa eommersial steel s = 0,00015 ft
sID = 0,00015/0,0874 = 0,00172
Dari fig 14-1 Peters and Timmerhaus 4ed diperoleh f= 0,009
Penafsiran panjang pipa lurus (.1L) = 5 m = 16,4042 ft
IlL v2
Ft=4f .-._-. D 2·ge
= 4.0 009. 16,4042ft . 2,48332
- 0 6475 , 0,0874 2·32,174 '
3. Losses karena friksi pada elbow dan valve, hf
Terdapat 2 elbow 90,1 globe valve
Prarencana Pabrik Asam Nitrat
AppendiksC
Dari Geankoplis tabel 2.10-4 :
Kf= 2 . 0,75 + 1. 6 = 7,5
h=Kf.( v2
) 2·a·gc
= 7,5 .( 2,48332
)= 0,7188 fl·lbf 2 ·1· 32,17 Ibm
4. Losses karena ekspansi, pada inlet bak
Dimana : A, = luas penampang pipa
Az = luas penampang bak
Karena A,«<Az maka A,/Az diabaikan
Kex = (1- ~: J = (1 - oi = 1
Hex = Kex. ( v2
) = 1. ( 2,48332
) = 0,0958 2· a . gc 2 ·1· 32,17
5.Losses karena pressure drop di bak penampung
PI = 14,7 psia = 176,4 lbf/ftz
P2 = 14,7 psia= 176,4Ibfi'~
AP=O
LF = 0,0527 + 0,6427 + 0,7188 + 0,0958 = 1,51 ft lbfi'lbm
1 z z g P2-P,. W.= ·(vz -VI)+ _·(Zz-Z,)+ + OF
2·a·gc gc p
Ws= 1 .2,4833 2 + 32,174flllbf·s2 .6+0+ 151 2.1.32,174 32,174 fl IIbf . S2 '
= 7,6058 ft.lbfi'lbm .
C-35
Efisiensi pompa (11) = 60% (Peters & Timmerhaus 4ed fig 14-37, p.520)
-w ·m Brake hp= s
1]·550
Bhp 7,6058 ·1,1157
0,0257 hp 0,6 ·550
Prarencana Pabrik Asam Nitrat
(Geank:oplis ed.3, pers.3.3-2)
Appendiks C C-36
Efisiensi motor = 80% (Peters & Timmerhaus 4ed fig 14-38, P 521)
Sehingga dipakai pompa dengan motor = 0,0257/0,8 hp = 0,0321 hp
Spesifikasi
Tipe
Rate aliran pompa
Power motor
Bahan konstruksi
Jumlah
14. ABSORBER (D-240)
: centrifugal pump
: 0,0169 fl?/s
: 0,0321 Hp
: stainless steel
: 1 buah
Fungsi : mengabsorbsi gas N02 menjadi HN03.
L2 G2
Gl L1
Reaksi Overall :
3N02(g)+H20 0) -------- 2HN03(08)+ NO(8)
Kondisi operasi
Suhu= 40 °c Tekanan = 9,5 atm
Prarencana Pabrik Asam Nitrat
AppendiksC
Menghitung diameter kolom
Gas masuk kolom, G I
KmoI/jam
NO = 1,4692
N02 = 28,6299
'N2 = 414,6227
O2 = 20,2845
H20 = 4,7210
469,7273 kmoI/jam
Komponen Fraksi mol
N02
N2
02
H2O
NO
Gas keluar kolom, G2
Kmol/jam
N02 = 1,4315
N2 = 414,6227
02 = 20,2845
NO = 10,5354
0,0610
0,8827
0,0432
0,0101
0,0031
446,8741 kmol/jam
Komponen Fraksi mol
N02 0,0032
N2 0,9278
O2 0,0454
NO 0,0236
Prarencana Pabrik Asam Nitrat
kg/jam
44,0764
1316,9767
11609,4364
649,1030
84,9785
13704,5710 kg/jam = 30212,899 Jb/jam
Fraksi berat
0,0961
0,8471
0,0474
0,0062
0,0032
kg/jam
65,8488
11609,4364
649,1030
316,0608
C-37
12640,449 kg/jam= 27866,9511Ib/jam .
Fraksi berat
0,0052
0,9184
0,0514
0,0251
Appendiks C
Laju alir liquid masuk kolom (L2) = 839,7682 kg/jam = 1851,34081b/jam
Liquid keluar kolom,Ll
RN03 = 18,1323 kmol/jam = 1142,3342 kg/jam
H2O = 42,3087 kmol/jam = 761,5561 kg/jam
60,4410 kmol/jam 1903,8903 kg/jam =4197,2890 Ib/jam
Komponen Fraksi mol Fraksi berat
RN03 0,3 0,6
H2O 0,7 0,4
Direncanakan Packed Column dengan memakai packing 1" keramik Rasching
Ring (RR).
Dari.Treyball, table 6.3 didapat.
Cf = 155
Wall thickness = 3mm
Co
gc
:= 301
=4,18.108
Menghitung diameter bagian Atas kolom
G2 keluar pada suhu 40°C. L2 masuk pada suhu 40°C.
G2 = 27866,449 Ib/jam
L2 = 1851,3408 Ib/jam
C-38
BM G2 = (0,0032.46)+(0,0236.30)+(0,0454.32)+(0,9277.28)=28,28IbIlbmoI
pG2 pada 3,38 atm dan 40°C (104OP),
G = 28,28. 460 + 32. 9,37 = 0 6651lb/ft? 2 359 460+86 I '
pL2 pada 30°C, PL= 0,993g/mol= 61,99Ib/ft? (Perry 6thed, table 3-28).
IlL2 = 0,73 cp = 1,771b/jam (Kern, fig 14)
I I
!:L( PG )2 = 1851,3408 ( 0,6651 )2 = 0 0069 G2 PL -PG 27866,449 61,991-0,6651 '
Prarencana Pabrik Asaro Nitrat
AppendiksC
Dari. Treyball, fig 6.34
G 2 C f.1. 0,1 J f' f' L" = 0,375
gC.pG,(PL - pJ
dimana Gr = rate massa pada kondisi flooding Ib/jam.tf
G/,(155XO,73r.1,502
( = 0 375
4,18.108XO,6651X61,99-0,6651) ,
Gr = 5280,37281b/jam.fh
Goperasi = 40-70% Gr
Diambil: Goperasi = 50%. Gr= (0,5.5280,3728)=2640,1864Ib/jam.tf
Luas Penampang Kolom
A = G2 = 27866,449 = 10,5559 jt Goperas; 2640,1864
Diameter Kolom
A = 1/41JD2 ~ 10,5559 = 1/41JD2
D = 4, 1667ft. :::: 4,5ft
R h· Ri D, 4,5.12 18" ase mg ng = 30 = 30 =,
Jadi diameter kolom bagian atas = 4,5ft
Menghitung diameter bagian bawah kolom
GJ = 30212,8991b/jam
LJ = 4197,2890 lb/jam
C-39
BM GJ = (0,0904.46)+(0, 7983.28)+(0,0447.32)+(0,0056.18)+(0,0031.30)
= 28,135Ib/lbmol.
G= 28,155.460+32.9,37 =06617/bljt3 P 359 460+86 1 '
pL = 0,9922 g/ml = 61,941b/ft3 (Perry 6ed, table 3-28 & 3-66)
pHN03= 1,3398 g/ml = 83,64lb/ft3
1 1 3 PL = X X 0303 0697 = 75,613/bl jt
_1 +_2 _'_+_'_ PI P2 61,94 83,64
Prarencana Pabrik Asam Nitrat
DA~pp~e~nd~ik~s~C~ ________________________________________ ~C-40
1lL1 pada 30°C (ilL)
llH2o= 0,657 cp = 1,5899Ib/jam.ft
IlHN03 = 1,7 cp = 4,114 lb/jam.ft
( Kern, figure 14 )
ilL = (Xl. IlLII3 + X2. IlLII3
) = (0,3.4,114 113) + (0,7. 1,58991/3)
= 1,314Ib/jam.ft
untuk:
I I
~( PG )2=4197,2890( 0,6617 )2=00123 GI PL - PG 30212,899 75,613-0,6617 '
dari figure 6.34, Treyball
G 2 0.1. f .Cf·f.J L .J.
-'---'---- = 0 25 gCPG ,(PL - PG) ,
G/. 155. 1,314°·1. 1,502. _ 8 -0)5
4,18.10 .0,6617.(75,613 - 0,6617)
Gr = 4654,2286 Ib/ft2.jam
Goperasi = 40 - 70 % (Perry 3ed, hal 674 )
Diambil Goperasi = 50 % Gr= 0,5. 4654,2286 = 2327,1143 Ib/ft2jam
Luas penampang kolom
A = GI/Goperasi = 30212,899 / 2347,1143 = 13,7774 ft2
Diameter kolom
A = 0,25.3,14. D2
13,7774 = 0,25.3,14. D2
D = 4,1894 ft = 4,5 ft
Rashing ring = D. tl30 = 4,5. 12/30 = 1,8"
Jadi diameter kolom bagian bawah = 4,5 ft
Menghitung tinggi kolom packing
Koefisien perpindahan massa fase Jiquida
KL.a = DAB.a..(Lllld-n.( IlUP.DAB)O,5
Prarencana Pabrik Asam Nitrat
Appendiks C
Untuk rasching ring eRR) I" harga a = 100 ; n = 0,22
_ ,16 112 T DAB -1,173.10 (cp.MB)' 06
JiL·9.1 . Dimana: kL.a = koefisien perpindahan massa fase liqui<ia,jam,1
L = rate air, ft3/ft2.jam
~L = viskositas air, lb/ft.jam
DAB = difusivitas gas N02 dalam air, ft2/jam
9A = volum molar solute N02 pada titik didih
p = densitas air, Ib/ft3
MB = berat molekul air lb/lbmol
T = suhu operasi, K
cp = association parameter dari air = 2,6
9A = 0,0156 + 2 (0,0074) = 0,0304 m3lkmol
D =1173.10,16(26.18)112. 30+273 AB, , 7,3.10-4.0,0304°,6
= 2,8.10,9 m2/s = 1,08.10-4 ~/jam
Rate air = 1857,36461b/jam
(Geankop1is, table 6.3-2)
Luas penampang kolom (A) = 0,25. 0.4,52 = 15,8963 ft2
Rate volumetric air = 1857,3646/61,99 = 29,9623 ft3/jam
L = 29,9623/15,8963 = 1,8849 ft3/~.jam
KL.a = 1,08, 1O-4.100,(1,884911,77t{),22.( 1,77/61,99.1,08.10-4)°,5
= 0,1844 jam,l
Koefisien perpindahan massa fase gas
Untuk RR 1" berlaku :
1<0. PI = 1,07 (JAP)-0,41(G.d)-0,41( Jia )-~ G Md· Jia pa.Da
Prarencana Pabrik Asam Nitrat
C-41
Appendiks C
Dimana : KG = koefisien perpindahan massa fase gas, Ib/ft2.jam.atm
G = rate gas, Ib/ft2.jam
Pf = rata-rata logaritmik tekanan parsial gas inert, atm
M = berta molekul gas, lb/lbmol
J..lG = viskositas gas, lb/ft.jam
PG = densitas gas, Ib/ft3
d = 1 in = 0,0833 ft
Dari figure 15, Kern :
J.LN02 = 0,019 cp
J.LNO = 0,016 cp
J.LN2 = 0,018 cp
J.Lo2 = 0,021 cp
J.LH20 = Om cp
J.lcampuran = (0,019.0,0904) + (0,016.0,0031) + (0,018.0,7983)
+ (0,021. 0,0447) + (0,01. 0,0056)
= 0,02 cp = 0,048 lb/ft.jam
G = 30212,899 20169281Ib/ft2.·am 158963 ' J ,
D _1.1O-7.r1,75.(1/MA
+I/MB
)IJ2
AB- P(Cr..9A
)IJ3 + (r..9Bi J3 i
Dimana : DAB = difusivitas gas A dan B, m2/s
T = suhu operasi, K
M = berat molekul, kglkmol
.9 = volum difussion
Untuk N02 - H20
Prarencana Pabrik Asam Nitrat
.9A = 16,65
.9B =12,7
C-42
Appendiks C
Pada bagian bawah kolom
Fraksi mol gas inert = 0,9133
Tekanan parsial gas inert = 0,9133.9,37 = 8,5576 attn
Pada bagian atas kolom
Fraksi mol gas inert = 0,9967
Tekanan parsial gas inert = 0,9967. 9,37 = 9,339 attn
Pf= 9,339 - 8,5576 = 89426 9339 ' atm
In ' 8,5576
C-43
2
Ko. 8,9426 = 1,07 (25)-O.41(2016,9281.0,0833)-O.41( 0,048 )-3 2016,9281 28,135 ' 0,048 0,6619.2,893.10-6
Ko = 0,1178 Ib/ft2.j am. attn
a = 1 8 cm-1 = 54 865 ft- I , ,
Ko.a = 0,1178.54,865 = 6,4620 Ib/ft3.jam.attn
Bagian bawah kolom
Tekanan parsial gas N02 = 0,0598. 9,37 = 0,5603 attn
KG.a .P A = 6,4620 .0,5603 = 3,6208 Ib/jam.ft2
Rate massa:
RN03 = 2518,3735 lb/jam = 39,9243 lbmol/jam
H20 = 1678,9156 Ib/jam
Pcampuran = 75,56131b/ft3
V = 2518,3735 + 1678,9156 55,4408 ft3/J'am campuran 75 613 ,
Konsentrasi RN03 (CB) = 39,9243/55,4408 = 0,7201Ibmol/ft3
KL.a.CB = 0,1844.0,7201 = 0,1328Ibmol/ft3.jam = 8,3655 Ib/ft3.jam
KL.a.CB> Ko.a.P A
Bagian atas kolom
Tekanan parsial gas N02 = 0,0032.9,37 = 0,02998 atro
KG.a.PA = 6,4620.0,02998 = 0,1938Ib/ft3.jam
Rate massa
Prarencana Pabrik Asaro Nitrat
AppendiksC
H20 = 1857,36461b/jam = 103,18691bmolljam
PH20 = 61,991b/ft3
Vcampuran = 18!~,~:08 = 29,9623 ft3/jam ,
Konsentrasi RN03 (CB) = 103,1869/29,9623 = 3,44391bmollft3
KL.a.CB = 0,1844.3,4439 = 0,6351Ibmol/ft3.jam = 11,4310 Ib/ft3.jam
KL.a.CB > KG.a.P A
eM
Karena KL.a.CB > KG.a.P A baik pada bagian atas maupun bawah maka yang
mengontrol adalah tahanan fase liquid
Untuk menghitung tinggi kolom packing:
H- ( G JI YT
- KL.a,CB
n YB
Dimana: H = tinggi kolom packing, ft
G = rate massa liquid, lb/~.jam
KL.a = koefisien perpindahan massa fase gas Ib/jam.ft3.atm
CB = konsentrasi, Ib/ft3
Y B = fraksi mol H2O pada bagian bawah kolom
Y T = fraksi mol H2O pada bagian atas kolom
H = (2016,9218)ln_1_ = 73,2574 ft 9,8186 0,7
Menghitung presure drop
L2 = 116,8429 Ib/ft2.jam
G 1 = 2016,9345 Ib/ft2.jam
= 28,155.460+32.9,37 =066171blfl3 PG 359 460+86 1 '
PL = 0,993 g/mol = 61 ,991b/ft3 ( Perry 6thed, table 3-28).
untuk rasching ring 1" m = 32,1 ; n = 0~00434 (Perry 6ed, hal 18-24)
Prarencana Pabrik Asam Nitrat
AppendiksC
!1P = 32,1.(10-8 ).(10°,00434.116,8429/61,99). 2016,93452
z ~~1
= 1,9947Ib/ft2.ft < 2,6 Ib/ft2.ft (memenuhi syarat)
Menghitung tebal kolom
Menggunakan bahan konstruksi carbon steel SA-283 grade C
P operasi = 9,37 atm = 137,739 psi =152,439 psig
P design = 1,2 . 152,439 = 182,9268 psig
Dari tabel13.l, Brownel & Young:
F allowable = 18750 Ib/in2
&=85%
P .. ri ts=---
f·c-0,6'p
165,2868. 54 2
18750 .. 0,85 - .0,6.165,2868
=02818 = ~ in , 8
Menghitung Tebal Head
Direncanakan :
- bahan konstruksi stainless steel SS
, - bentuk head eliptical dished head
(Brownel & Young, pers 13.1)
Harga k = 2 (Brownel & Young, hal 133 )
V = 116 ( 2 + k2 )
= 116 ( 2 + 22 ) = 1
h P .. d .. v
t =----2f·c-0,2.P
165,2868 .. 54
2 .. 18750.0,85 - 0,2 .. 165,2868
= 0 2803 = ~ in , 8
Prarencana Pabrik Asam Nitrat
C-45
DA~~~~eillndlliik~s~C~ ________________________________________ ~C46
Menghitung tinggi head
dari table 5.11 Brownell & Young,
sf= 3 in
tinggi head =(ID/4) + sf + t
= 3 + 0,2803 + (54 14) = 16,7803 in = 1,3984 ft
Spesifikasi :
Bahan : stainless steel
Diameter : 4,5 ft
Tinggi tanki total : 76,0542 ft
Tinggi tutup atas : 1,3984 ft
Tinggi tutup bawah : 1,3984 ft
Tebalshell : 3/8 in
Tebal tutup atas : 3/8 in
Tebal tutup bawah : 3/8 in
Jumlah : 1 tanki
15. HEAlER (E-233)
T2 392or' condensat
t2 = 356or' heater
gas t1 = 104bF ~ L.." ____ -.--'
TI 392or' steam
Fungsi : untuk memanaskan gas recycle dari abosrber
Tipe : shell and tube
Perhitungan :
Neraca Panas
m gas = 6320,2245 kg/jam = 13933,4755 Ib/jam
M steam = 273,7055 kg/jam = 603,4071 lb/jam
Prarencana Pabrik Asam Nitrat
~A~pp~en~d~ik~s~C __________ ~ __________ ~ ________________ ~C~7
Q = 531193,8592 kkal/jam =2107912,14 btu/jam
LTMD (392-104)-(392-356) = 121 1864"F In (392 -104) ,
Llt= 121,1864 of
Tc = 392°F
(392-356)
tc = (104 +356)/2 = 230°F
Trial UD = 10
A = Q = 2107912,14 378,9163 Ud.LlT 10.121,1864
Ditetapkan:
OD tube = 1 in, 10 BWG
ID tube = 0,732 in
L = 12 ft
a" = 0 2618 ff ,
( Kern, table 10)
lumlah tube = ~= 378,9163 = 120,6125 a" . .L 0,2618 .. 12
Dari tabel 9 Kern, untuk square pitch
1 . Pr= 1-m
4
Nt standar = 122 buah
Passes =6
ID shell = 19,25 in
k k · 120,6125 10 97 25 UDter ore SI= = ,7 122
Shell, steam
1 1 C' =Pr-OD= 1--1 =-
4 4
Tube, gas
a't = 0,421 (tabel 10)
3 B= -.19,25= 14,4375 at = Nt .. a't - 122xO,421_ 0,0594 ft2
144 .. n 144x6 4
Prarencana Pabrik Asam Nitrat
AppendiksC
!D .. c'.E '/ls =
144.Pr
19,25. ~ .14,4375
144.1!
= 0,3860 ff
Gs = W = 603,4071 as 0,3860
4
= 2848,5106 lb/jam ft
Pada Ie = 392°F
j.1= 0,0165.2,42 = 0,03991b/jam ft
(fig. IS)
De = 0,72112 = 0,06
e=0,49
k = 0,0187
(fig. 28)
(fig. 3 )
(tab. 5)
Res = D.Gt = 0,06.2848,5106 J.I. 0,029
=4283,4746
jH=35 (fig, 28)
I I
(C.p )3 =(0,49.0,0399)3 = 1 0149 k 0,0187"
I
~ = jH(~SXC:)3
= 35 0,018710149= 11 0709 006 ' , ,
Prarencana Pabrik Asam Nitrat
C-48
Gt = ~= 13933,4775 at 0,0594
= 234592,9798 lb/jam ft
Pada tc = 230"F
j.1 = 0,034 . 2,42 = 0,0823 lb/jam ft
(fig. 14)
e = 0,2878 (fig. 2 )
k= 0,0369
D = 0,732112 = 0,061 ft
(tab. 4)
(tab. to)
Ret = D.Gt = 0,061.234592,9798 p 0,0,0823
= 173878,1503
!:... = ~ = 196 7213 D 0,061 '
jH = 400 (fig. 24)
I 1,
(C.p)3 =(0,2878.0,0823)3 = 08626 k 0,0369 '
1
hi _ 'H( k XC.J.I.)3 --j - --¢t D k
= 400 (0,0369}0 8626 0,061 '
= 208,7209
hio = hi. !D = 2087209. 0,732 ¢t ¢t OD ' 1
= 152,7837
Appendiks C
ko
tw=tc+ . r/JS (Tc-tc) h/O ho -+-t/X r/JS
= 230+ 11,0709 (392-230) 152,7837 + 11,0709
= 240,95"F
Pada tw = 240,95"F
J..1w = 0,018.x 2,42 = 0,0436 (fig.15)
C-49
pada tw = 240,95"F
J..1w = 0,035.x 2,42 = 0,0847
(fig. 14)
r/JS = (£)0,14 = (0,0399)°·14 = 0,9877 t/X = (£)0,14 = (0,0823)°'14 = 0,996 f.JW 0,0436 f.JW 0,0847
ho = 11,0709 x 0,9877 = 10,9347 hio = 152,7837 x 0,996 = 152,1726
Uc = kio .. ko = 10,9347 .. 152,1726 10,2016 hio + ho 10,9347 + 152,1726
Rd= Uc-UD = 10,2016-9,7725 0,0043 Uc"UD 10,2016.9,7725
(memenuhi> 0,003)
Perhitungan pressure drop
Shell, steam
Nres = 4283,4746
f=0,0017
L 12 N+l = -.12= -.12= 192
B 75 ' ,
p steam = 0,0592 Ib/ft3
Tube, gas
Nret = 173878,1503
(fig. 29) f= 0,00013
BM gas = 28,28 kglkmol
(fig. 26)
P.BM 9,37.28,28 p gas = R.T 0,0821.503
(Geankoplis, Tabel A-3.3)
s = 0,0592 - 0 00095 625 '
= 6,4166 kg/m3 = 0,4010 Ib/ft3
,
Prarencana Pabrik Asam Nitrat
Appendiks C
IDs = 10 in =0,8333 ft
AD _ f·Gs 2.IDs.(N + 1) UFS - 10
5,22.10 De.s.¢AY
= 0,0028(2848,51 06f 1,6042.9,974
5,22.1010.0,06.0,00095.0,9987
= 1,1223 psi
(memenuhi < 10 psi)
Spesifikasi:
Tipe : shell & tube
s = 0,4010/62,5 = 0,0064
AD _ j.GP.L.n tlJt- 10
5,22.10 D.s.t/X
C-50
, = 0,00013(234592,9798i.12.6
5,22.1010.0,061.0,0064.0,996
=0,2538 psi
v -=0007 2g' '
4n v .1Pr=--
s 2g'
(fig. 27)
4.6 0,007 = 1,625 psi 0,0064
I'lPr = 0,2538 + 1,625 = 1,8788 psi
(memenuhi < 2 psi)
Shell: ID = 19,25 in; baffle space = 14,4375 in; passes = I
Tube: OD = 1 in; 10 BWG; L = 12 ft; passes = 6; Pr = I ! in (square pitch)
J umlah tube : 122
Ud = 9,7725
Uc = 10,1026
Rd= 0,0043
M shell = 1,8788 psi
M tube = 1,1223 psi
16. EKSPANDER (G-250)
Fungsi : untuk memperkeciI tekanan gas buang
P input = 9,5 atm = 9,5 bar
P output = I atm = 1 bar
Prarencana Pabrik Asaro Nitrat
Appendiks C
Massa = 6320,8357 kg/jam = 1,7558 kg/s
Asumsi effisiensi = 55%
as = P.BM = 9,5.28,28 = 10 7998 kg/m3
P g R.T 0,0821.303 '
Ws = s.m.(pl- p2) (Ulrich hal.93 pers.4-19) p
= 0,55 .. 1,7558 .. (9,5 -1).105
76004,7871 J/s = 76,027 Kw 10,7998
Spesifikasi :
Tekanan masuk
Tekanan keluar
Rate gas
Ws
Jumlah
Praiencana Pabrik Asam Nitrat
: 9,5 bar
: 1 bar
: 1,7558 kgls
: 76,027 Kw
: 1 buah
C-51
Appendix D. Perhitungan Analisa Ekonomi 0- I
APPENDIX D
PERIllTUNGAN ANALISA EKONOMI
Harga alat akan berubah setiap saat tergantung pada kondisi ekonomi
dan politik, untuk itu dibutuhkan suatu metode yang dapat dipakai untuk
mengkonversi harga alat pada beberapa tahun yang lalu agar dapat diperoleh
harga alat yang ekivalen pada saat ini.
Ekivalensi itu dapat dihitung dengan menggunakan persamaan :
.. indeks h arg a saat ini Harga alat tahun lUI = x harga alat tahun A
indeks h arg a tahun A
Harga alat pada tahun A diperoleh dari literatur Peters & Timmerhaus.
Sedangkan indeks harga tersebut adalah :
Chemical Engineering Plant cost index
• Tahun A (Januari 1990) = 356 (tabel3, hal 163, Peters & Timmerhaus)
• Saat ini (Januari 2002 ) = 394,3 ( Chemical Engineering, Januari 2002 )
D.l. Perhitungan Barga Peralatan
Contoh perhitungan :
Tanki penampung NH3 (F-1IO)
Kapasitas = 2617,9574 ft3 = 19582,3214 gal
HargaJanuari 1990 = $ 220.000 ( fig 14-56, hal 539, Peters & Timerhaus )
Harga alat saat ini = 394,3 x220000 = $ 243.668,54 356
Prarencana Pahrik A~am Nitrat
Appendix D. Perhitungan Analisa Ekonomi D-2
Dengan cara yang sarna didapatkan harga alat yang lain seperti pada tabel 1.1.1.
Tabel D.l.l Harga Peralatan Proses
No. Namaalat Kode Jumlah Harga, $
I Tangki penampung NH3 F-IIO 2 243.668,54
2 Filter udara H-120 1 5.537,92
3 Kompresor G-121 1 360.265.63
4 ~ompresor G-122 1 360.265.63
5 lFurnace Q-211 1 521.516,85
6 Oksidator I R-210 1 632.275,28
7 Gas-gas heat exchanger E-214 1 8.306,88 ,
8 Bag filter H-220 1 44.366,85
Cj Blower 2 G-231 1 88.606,74
10 Oksidator 2 E-230 1 295.756.42
11 Condensor E-232 1 9.968,26
12 Blower 3 G-241 1 7.753,09
13 ~bsorber D-240 4 949.111,72
14 Heater E-233 I 11.075,84
15 Pompa 3 L-311 1 1.107,58
16 rranki penampung HN03 F-3IO 1 232.592,7C
17 ~kspander G-250 1 160.265,63
Total harga alat 3.935.441,56
Prarencana Pllhrik Asam Nitrat
Appendix D, Perhitungan Analisa Ekonomi D- 3
Tabel D.l.2. Harga Peralatan Utilitas
No. NamaAlat Kode Jumlah Harga, $
1 rrangki sand filter H-355 2 10.522,56
2 rrangki demineralisasi D-366 2 ~2.088,20
3 ~angki koagulator dan flokulator H-353 1 ~6.718,75
4 !Pompa air sumur L-350 1 1.100,00
5 !Pompa air ke bak koagulator L-352 1 1.100,00
6 Pompa L-358 1 1.700,00
7 Pompa air ke bak pendingin L-364 1 1.250,00
9 Pompa air pendingin L-366 1 1.200,00 ,
10 Pompa air proses L-360 1 1.200,00
11 !Pompa air sanitasi L-362 1 1.000,00
8 Cooling tower E-363 1 16.440,70
9 ~enerator 1 41.200,57
10 Boiler 1 15.482,81
Total harga alat 161.003,59
Prarencana Pabrik Asam Nitrat
Appendix O. Perhitungan Analisa Ekonomi 0-4
Tabel D.l.3. Bak Utilitas
No. Nama Peralatan Kode Jumlah Luas, m2
1 Bak air sumur F -351 1 87,12
2 Bak pengendapan H-353 1 93,80
3 Bak air bersih F-357 I 47,00
4 Bak umpan air boiler F-367 1 9,35
5 Bak air pendingin F-365 1 167,9
6 Bak air proses F-359 1 11,16
7 Bak air sanitasi F -361 1 11,88
Total 428,21
Harga bak = Rp. 250.000,-/m2
Total harga bak utilitas = (Rp. 250.000,- 1 m2) '" 428,21 m2 = Rp. 107.052.500,
Total harga peralatan = $ 3.935.441,56+ $ 161.003,59+ Rp. 107.052.500,-
= ($ 4.096.445,15 x Rp. 9500,-1$) + Rp. 107.052.500,- ,
= Rp. 39.023.281.430,-
D.2. Perhitungan Barga Tanah dan Bangunan
Luas tanah = 10.000 m 2
Harga tanah = Rp. 500.0001 m2
Harga total tanah = 10.000 x Rp. 500.000 = Rp. 5.000.000.000,
Luas bangunan kantor = 350 m2
Harga bangunan = Rp.l.OOO.OOO,-
Prarencana Pabrik Asam Nitrat
L
Appendix D. Perhitungan Analisa Ekonomi
Harga total bangunan = Rp. 350.000.000,
Luas bangunan lain - lain = 3254 m2
Harga bangunan = Rp. 500.000,-
Harga total bangunan lain -lain = Rp. 1.627.000.000,
Luas Pabrik dan gudang = 950 m2
Harga bangunan pabrik = Rp. 800.000,-
Harga total bangunan pabrik = Rp. 760.000.000,-
Harga total tanah dan bangunan = Rp. 5.000.000.000 + Rp. 350.000.000 +
Rp. 1.627.000.000 + Rp. 760.000.000
= Rp. 7.737.000.000,-
D.3. Perhitungan Barga Bahan Baku dan Produk
1. Harga Bahan baku
• NH3
Harga = Rp. 1.750,- / kg
Kebutuhan = 32.174,5260 kg / hari
Total = Rp. 56.305.420/ hari = Rp. 18.580788.770.,- / tahun
• Katalis Pt
Harga = Rp. 50.000.000,- / kg
Kebutuhan= 0,1130 kg /14 hari
Total = Rp. 5.650.000/ 14 hari = Rp. 133.178.572,- / tahun
D-5
Totalhargabahanbakupertahun =Rp. 18.S80.788.770+Rp. 133.178.572
= Rp. 18.713.967.340,-
Prarencana Pabrik Asam Nitrat
Appendix D. Perhitungan Analisa Ekonomi
2. Harga jual
• HN03
Harga = Rp. 10.000,- / kg
Produksi = 1901,5133 kg / jam = 45.636,3192 kg / hari
Total = Rp.456.363.192,- / hari
= Rp. 150.599.853.400,- / tahun
D.4. Perhitungan Gaji Karyawan
Upah./bulan,
No Jabatan Jillnlah Rp
1 iDirektur Utama 1 10.000.000
2 pirektur Teknik dan Produksi 1 6.000.000
3 iDirektur Administrasi & Keuangan 1 6.000.000
4 Sekretaris 3 1.500.000
5 ~abag Produksi 1 4.000.000
6 Kabag Teknik 1 4.000.000
7 KabagUmum 1 4.000.000
8 Kabag Pemasaran 1 4.000.000
9 [Kabag Administrasi & Keuangan 1 4.000.000
10 iKasie Proses 1 2.500.000
11 iKasie Utilitas 1 2.500.000
12 jKasi Laboratorium 1 2.500.000
13 ·iKasi Maintenance 1 2.500.000
D-6
Total, Rp
10.000.000
6.000.00C
6.000.00C
4.500.000
4.000.000
4.000.000
4.000.q.OO
4.000.000
4.000.00C
2.S00.00C
2.500.00C
2.500.0OC
2.500.00C
Appendix D. Perhitungan Analisa Ekonomi D- 7
14 lKasi Personalia 1 2.500.000 2.500.000
15 iKasi Keamanan 1 2.500.000 2.500.000
16 lKasi Pemasaran 1 2.500.000 2.500,,o0(
17 lKasi Gudang 1 2.500.000 2.500.00(
18 iKasi Keuangan 1 2.500.000 2.500.00(
19 lKaryavvanProses 36 800.000 28.800.000
20 lKaryavvan Utilitas 9 800.000 7.200.000
21 lKaryavvan Laboratorium 6 800.000 4.800.00C
22 iKaryavvan Maintenance 9 800.000 7.200.00C
23 lKaryavvan Personalia 4 800.000 3.200.000
24 lKaryavvan Keamanan 12 600.000 7.200.000
25 lKaryavvan Pemasaran 5 800.000 4.000.000
26 lKaryavvan Gudang 9 750.000 6.750.000
27 iKaryavvan Keuangan 3 800.000 2.400.000
28 lKaryavvan Litbang 1 800.000 800.000
29 Sopir 4 600.000 2.400.000
30 ITukang kebun 2 500.000 1.000.000
Total = 120 144.750.000
Gaji karyavvan per bulan = Rp. 144.750.000,-
Ditetapkan satu tahun produksi adalah 12 bulan ditambah 1 bulan tunjangan untuk
hari raya. Jadi gaji karyavvan per tahun adalah = Rp. 144.750.000 * 13 bulan
= Rp. 1.881.750.000,-
Appendix D. Perhitungan Analisa Ekonomi D- 8
D.S. Perhitungan Biaya Utilitas
1. Kebutuhan Air
Air yang harns disuplai per hari = 442,7916 m3
Harga pengolahan Air Sumur = Rp. 300,-
Biaya air per tahun = ( 442,7916 m3 / hari * Rp.300,- / m3
) x 330 hari/tahun
= Rp.43.836.368,4,-
2. Kebutuhan Alum
60 menit 1 Kebutuhan alum per hari = 1,1148 kg * * * 24 jam
jam 25 menit
= 64,2125 kg
Harga alum = Rp. 3000 / kg
Biayaalum pertahun =Rp. 3000 * 64,2125 *330
= Rp. 63.570.356,-
3. Kebutuhan Listrik
Kebutuhan listrik total = 1831,1374 KW
Beban listrik terpasang = 1,2 * 1831,1374 KW = 2197,3649
Biaya beban per bulan = Rp. 25.000,-
Biaya beban per tabun = 12 bulan * Rp. 25.000,- / bulan * 2197,3649
= Rp. 659.209.470,-
Biaya listrik : WBP = Rp. 455,- / KW (pk. 18.00 - 22.00 )
L WBP = Rp. 350,- / KW (pk. 22.00 - 18.00 )
n .......... _ ...... __ n ... t.. ... :1,... A .... _ ltt"T: ....... +
Appendix D. Perhitungan Analisa Ekonomi D-9
Biaya Iistrik terpakai per tahun :
= [(( 4 jam * 2197,3649 KW * Rp. 455,- / KW) + (20 jam * 2197,3649 KW *
Rp. 350,- / KW )) * 330 hari / tahun] + [ (( 4 jam * 15,73 KW *
Rp.455,- / KW + ( 20 jam * 15,73 KW * Rp.350,- / KW)) * 365 hari / tahun]
= Rp. 5.129.453.030,-
Biaya Iistrik total per tahun = biaya beban + biaya listrik terpakai
4. Kebutuhan bahan bakar
= Rp. 659.209.470,- + Rp. 5.129.453.030,
= Rp. 5.788.662.500,-
Kebutuhan bahan bakar IDO per bulan = 50467 It
Harga bahan bakar per liter = Rp. 1. 133,-
Biaya bahan bakar per tahun = 50467 It / bIn * 12 bin / th x Rp.1. 133
= Rp. 686.500.035,
Harga solar per liter = Rp. 1.860,-
Kebutuhan solar per bulan = 3473,63 It
Biaya bahan bakar per tahun = 3473,63 It / bin * 12 bin / th x Rp.l.860
=Rp.77.531.421,-
Total biaya bahan bakar per tahun = 77.531.421 + 686.500.035
= Rp. 764.031.456,-
Kebutuhan bahan bakar LNG per bulan = 292.804,56 kg = 645.512,69 Ib
= 187.269,6181 gal
= 708.817,631 It
Appendix D. Perhitungan Analisa Ekonomi D - 10
Harga bahan bakar per liter = Rp. 500,-
Biaya bahan bakar per tahun = 708.817,631 It / bin * 12 bin / th x Rp.500"
= Rp. 4.252.905.786,-
Biaya total bahan bakar = Rp. 764.03l.456 + Rp. 4.252.905.786
= Rp. 5.016.937.242,-
Total biaya utilitas per tahun :
= Rp. 63.570.356 + Rp. 12.282.l00.970 + Rp. 5.016.937.242
= Rp. 17.362.608.570,-
Prarencana Pabrik Asam Nitrat
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